High Protein Organic Materials as Fuel and Processes for Making the Same

ABSTRACT

A process of making a fuel product from a non-combustible high protein organic material such as a biological by-product or waste material. The moisture content of the high protein organic material is mechanically reduced and dried to reduce the moisture content to less than ten percent (10%). The high protein organic material is pulverized to a particle size of less than about 2 mm. The high protein organic waste material is fed into a combustion chamber and separated during combustion such as by spraying of the high protein organic waste material within the combustion chamber. Temperature and nitrogenous hydrocarbon combustion reactions within the combustion chamber are also controlled by injection of steam within the combustion chamber. The concentration of protein thermal decomposition by-products, the temperature and/or pressure within the combustion chamber is also controlled to degrade hazardous polyfluoro compounds into less hazardous compounds.

The present application is a Continuation-in-Part of and claims priority to U.S. application Ser. No. 16/345,151 filed on Apr. 25, 2019 which is a national stage entry of International Application No. PCT/US17/30420 filed on Apr. 30, 2017, which claims priority to International Application No. PCT/US16/59528 filed on Oct. 28, 2016 and U.S. application No. filed on Mar. 24, 2017, now issued as U.S. Pat. No. 10,781,388, which is a Continuation-in-Part of and claims priority to U.S. application Ser. No. 14/756,904 filed on Oct. 28, 2015, now issued as U.S. Pat. No. 10,364,400, which is a Continuation-in-Part of and claims priority to U.S. application Ser. No. 13/199,505, filed on Sep. 1, 2011, now issued as U.S. Pat. No. 9,447,354, all of which are herein incorporated by reference in their entireties.

TECHNICAL FIELD

The present disclosure generally relates to organic materials that are problematic to burn because of their high protein content. Such materials include bio-solids from waste water treatment plants; high protein fermentation waste and waste by-products; high protein waste and by-products from agricultural sources of oil production; and high protein meat production waste, high protein meat by-products, high protein biological waste by-products and high protein animal excreta. These potential fuels are too high in protein to allow for suitable combustion under typical conditions and to allow for regulatory compliant emission characteristics in combustion chambers such as those used to make Steam. While these high protein organic materials can burn they are unable to sustain unassisted auto combustion in air once ignited. These high protein organic materials are traditionally considered non-auto combustible. While wood products and petroleum products can sustain unassisted auto combustion once ignited in air, these high protein organic materials will stop burning if additional fuel is not used to assist in their incineration. These high protein organic materials maybe able to be burnt (incinerated) however, they are not able to sustain an auto combustible state without additional traditional fuels being use (e.g. wood products, paper products, cardboard, high cellulosic bio-mass such as grass or hay or chaff etc., or hydro carbons such as fuel oil, coal or natural gas). Accordingly, the present disclosure relates to a novel and improved process for making a combustible fuel product from a traditionally considered non-auto combustible organic material that is high in protein. The present disclosure further relates to the novel use of high protein organic materials as a primary fuel source for a furnace, steam boiler, incinerator and other combustion applications and to a method of using protein thermal decomposition by-products to degrade hazardous compounds to less hazardous substances and/or extraordinarily stable compounds not normally degradable in conventional combustion operations.

BACKGROUND

Certain high protein organic materials are known for being problematic when used as a source of fuel. Such materials may be ignited, however, they have not been previously shown to auto-combust as previous attempts to use these high protein materials as a primary fuel for combustion results in incomplete combustion and/or the generation of a large amount of smoke which is outside of regulatory compliance limits, for example, exceeding 20% opacity averaged over 6 minutes (i.e., more than 20% of light is blocked by emissions over any 6 minute interval).

Consequently, the only way these high protein organic materials could be used for continued combustion over an extended period of time is when these materials constituted only a minor component of the total fuel used in the combustion chamber. Ultimately, traditionally high protein organic materials needed other traditional flammable materials (e.g., wood products, paper products, cardboard, high cellulosic bio-mass such as grass or hay or chaff etc., or hydro carbons such as fuel oil, coal or natural gas) to constitute the majority of the fuel that is used for combustion. These high protein organic materials, however, present great potential for reducing operating costs of fuel operated systems, conserving use of other fuel sources and for disposing unwanted materials. Examples of high protein materials which have been traditionally problematic as alternative fuel sources include but are not limited to grains such as spent grain and distillers grains, hops residues, yeast residues, solid waste material from animals, bio-solids from waste water treatment plants, high protein animal meat processing by-product (e.g., meat and bone meal, feathers, feather meal, animal excreta) and other high protein organic wastes and high protein organic by-products.

Spent grain from the brewing of alcoholic products has been used as a food product such as cattle feed. In some of the processes used to make the food product, it is known to reduce the moisture content of the spent grain through press and/or drying operations. Although there have been some attempts to use spent grain as a major part of the fuel used for a steam boiler, such attempts have been unsuccessful due to insufficient or failure of combustion and excessive smoke produced thereby. Although there have been some successful attempts to use spent grain as a minor part of the fuel for a steam boiler or combustion system, attempts to use spent grain as the sole or primary fuel have been unsuccessful due to insufficient or failure of combustion and excessive smoke produced thereby.

Similar problems have been shown to exist with respect to the use of bio-solid waste materials from waste water treatment plants, animal solid waste, hops residues, oil seed pulp meal, high protein animal meat processing by-product (e.g., meat and bone meal, feathers, feather meal and animal excreta) and other high protein organic wastes as a primary fuel source. One feature that is common to these types of organic materials is that each of these materials contain a relatively large amount of protein and other compounds which cross link and agglomerate during combustion resulting in a relatively incomplete and inefficient combustion process. Therefore, what is needed is a process which can reduce the extent of the protein cross linking and other cross-linking reactions which result in the formation of larger agglomerated masses that occurs within these materials during combustion to render them suitable for use as an alternative fuel source.

Accordingly, the present disclosure provides a novel process for making a fuel product from a high protein organic material such as spent grain, distillers grains, hops residue, bio-solids from waste water treatment plants, solid animal waste, oil seed pulp meal, high protein animal meat processing by-product (e.g., meat and bone meal, feather meal, animal excreta) and other high protein organic wastes or combinations thereof. The present disclosure also provides a novel and improved process for making such fuel products. The fuel products included herein can be used in a furnace, a steam boiler, an incinerator or other fireboxes in conformance with present day environmental and emission laws and regulations. The fuel products included herein can also be successfully used as the sole or primary fuel for a steam boiler such as that used in the brewing process as well as other processes, drying operations, energy generation and other applications.

The present disclosure further provides a novel and improved process for making high protein organic materials as a fuel product using machines or devices that are commercially available in industry.

The present disclosure further provides heat for a brewing processes and other heat-required applications using a steam boiler fueled by novel high protein organic material as a fuel product made from the spent grain, distillers grains and hops residues by-products of the brewing industry.

The present disclosure also provides for fuel operated systems of various applications which incorporate the use of novel high protein organic materials as a fuel product made from bio-solids from a waste water treatment plant.

The present disclosure also provides for fuel operated systems of various applications which incorporate the use of novel high protein organic materials as a fuel product made from oil seed pulp meal.

The present disclosure also provides for fuel operated systems of various applications which incorporate the use of novel high protein animal meat processing by-products (e.g., meat and bone meal, feather meal, animal excreta)

The present disclosure also provides for fuel operated systems of various applications which incorporate the use of novel fuel products made from any high protein organic materials.

The present disclosure also provides for a process for combusting a traditionally non-auto-combustible high protein organic material using the non-auto-combustible high protein organic material as the sole or primary source of fuel, that is, without the use of a traditional combustible fuel or additives to aid in combustion (which include for example wood products, paper products, cardboard, high cellulosic bio-mass such as grass or hay or chaff etc., or hydro carbons such as fuel oil, coal or natural gas).

In addition, many non-autocombustible high protein organic fuels contain man-made toxic chemicals. These toxic chemicals are highly fluorinated and known as “forever chemicals” because they are nearly indestructible and last forever. “Forever chemicals” are used in manufacturing processes and in many consumer products such as nonstick cookware, food packaging, fire retardants (e.g., fire retardants used at air ports). They are also used in products such as sealant tape, floor wax, in machinery to reduce gear friction and to make clothing stain and water resistant (e.g., Scotchguard). “Forever chemicals” ultimately find their way into the water system and are ingested by both humans and animals. As such, high protein solids from waste treatment plant are known for containing “forever chemicals”. Accordingly, the present disclosure also provides a method of using protein thermal decomposition by-products to degrade extraordinarily stable hazardous compounds, such as PFAS to less hazardous substances and/or extraordinarily stable compounds not normally degradable in conventional combustion operations.

SUMMARY

Provided is a process for making a combustible fuel product from a non-auto-combustible organic material for a combustion system having a low nitrogen oxide (NOX) production and a low emissions opacity. The process includes the following steps in any order: providing a non-auto-combustible organic material, wherein the organic material is a high protein organic material having a protein content of about 10% (dry weight basis) or greater; optionally mechanically removing liquid and soluble components from the high protein organic material; optionally, applying heat to dry the organic material to reduce its moisture content to ten percent (10%) or less by weight; pulverizing the high protein organic material to reduce the high protein organic material to a particle size of less than 2 mm; separating particles of the high protein organic material during a combustion phase to inhibit their cohesion into an integrated mass by spraying the particles into a combustion chamber; simultaneously injecting steam into the combustion chamber to enhance combustion characteristics of the high protein organic material in a regulatory compliant manner; and, allowing protein thermal decomposition by-products to react with nitrogen oxides (NOX) within the combustion chamber to form water (H₂O) and nitrogen (N₂), wherein the nitrogen oxide (NOX) production ranges from about 100 parts per million (ppm) to about 150 parts per million (ppm) and wherein the opacity of the emissions is about 20% or less on average for every 6-minute interval. In further aspects of the present process, the nitrogen oxide (NOX) production is less than 150 parts per million (ppm) whereas in other aspects, the nitrogen (NOX) about 150 parts per million (ppm) or less. In certain aspects of the present process, the opacity of the emissions is about 20% or less on average for every 6-minute interval and in further aspects of the present process, the opacity of the emissions is about 6% or less on average for every 6-minute interval.

According to one aspect of the process, pulverizing, pressing, applying heat to dry the high protein organic material particles, spraying particles into the combustion chamber and injecting steam into the combustion chamber degrades the proteins contained within the particles and denatures them by allowing nitrogen cross-linking and other cross-linking reactions to occur within the particles, allowing the particles to complete all of the cross-linking ability before the particles contact other particles.

According to another aspect of the process, cross-linking of the high protein organic material particles is prevented by prematurely initiating cross-linking reactions of the nitrogen bonds and other cross linking reactions while the particles are being agitated and wherein the high protein organic material particles no longer adhere to each other, thereby arresting the particles tendency to adhere to each other within the combustion chamber via nitrogen bond cross-linkage and other cross-linking reactions.

According to another aspect of the process, the step of separating the high protein organic material by spraying the processed high protein organic material into the combustion chamber is effected through use of a pneumatic stoker.

According to another aspect of the process, spraying the particles of the high protein organic material into the combustion chamber by the pneumatic stoker keeps the particles separated in the combustion chamber long enough to allow heat transfer provided by the combustion process to quickly dry and then degrade proteins present within the high protein organic material and to prevent nitrogen cross linking and other cross linking reactions between the particles that would have the particles adhere to each other.

According to another aspect of the process, the particles of the high protein organic material are separated and dispersed within the combustion chamber and ignited and burned while in suspension and separated from each other before they land and adhere to each other.

According to another aspect of the process, the non-auto-combustible high protein organic material is rendered combustible without the addition of other combustible fuels or additives.

According to another aspect of the process, protein thermal decomposition by-products include ammonia, nitrogenous hydrocarbons and nitrogen-based compounds and wherein injection of ammonia, nitrogenous hydrocarbons and nitrogen-based compounds into the combustion chamber is not required to lower NOX production.

According to another aspect of the process, the step of removing water, moisture and other soluble components from the biological waste material incorporates the use of flocking agents, centrifuges, filter beds and dewatering separators.

According to another aspect of the process, the high protein organic material is a biological waste or by-product material.

According to another aspect of the process, the biological waste or by-product material originates from waste water treatment activated sludge waste. The process according to this aspect includes the following order of steps: 1) providing a biological waste material or by-product comprising a waste water treatment activated sludge having a protein content of about 10% or greater, on a dry weight basis (DWB) or in some cases, greater than 20%, on a dry weight basis (DWB); 2) removing water, moisture and other soluble components from the biological waste material or by-product; 3) drying the biological waste material or by-product to reduce the moisture content to 10% or less by weight; 4) pulverizing the biological waste material to reduce the particle size to be less than 2 mm; and 5) separating particles of the biological waste material or by-product during the combustion phase to inhibit their cohesion into an integrated mass by spraying the particles into the combustion chamber and 6) simultaneously injecting steam into the combustion chamber, wherein steam is injected to modify and control combustion reactions by reacting with nitrogen within proteins to form intermediate nitrogenous-based protein thermal combustion products which help to maintain regulatory compliance of combustion emissions.

According to another aspect of the process, the step of removing of water from the biological waste material or by-product comprises application of heat.

According to another aspect of the process, the step of drying biological waste or by-product material comprises drying the biological waste material or by-product in a heated drier, a heated progressing filter belt or other suitable drier and wherein the step of pulverizing the biological waste material or by-product comprises subjecting the biological waste material or by-product to a mill.

According to another aspect of the process, the high protein biological waste material or by-product is pulverized prior to drying to ensure that the high protein biological waste material has a particle size less than 2 mm.

According to another aspect of the process, the high protein organic biological waste material is hops residue. The process according to this aspect includes the following steps in the following order: 1) extracting oils and other compounds from the ground hops utilizing mechanical separation techniques or CO₂ extraction to obtain a high protein hops waste residue having a protein content of about 25 to about 30 weight percent, on a dry weight basis (DWB); 2) providing the hops waste residue 3) drying the hops waste residue; 4) grinding the hops waste residue into a powder by pulverizing the hops waste residue to ensure that particles of the hops waste residue have a particle size of less than 2 mm; 5) agitating the hops waste residue during a combustion phase to separate particles of the hops waste residue by spraying the particles into the combustion chamber to inhibit their cohesion into an integrated mass and 5) simultaneously injecting steam into the combustion chamber to enhance the combustibility of the high protein organic material.

According to another aspect of the process, the step of pulverizing the hops waste residue includes subjecting the hops residue to a mill and wherein the step of drying the hops waste residue comprises the application of heat.

According to another aspect of the process, the high protein organic material is a high protein waste or meal from an agricultural source of oil production, waste by-products and by-products from an oil seed pulp processing.

According to another aspect of the process, the biological waste material comprises an oil seed pulp waste residue. The process for making a combustible fuel product from oil seed pulp waste residue according to this aspect includes the following order of steps: 1) obtaining an extracted high protein oil seed pulp waste residue having a protein content of about 35%, on a dry weight basis, a moisture content of ten percent (10%) or less and a particle size less than 2 mm, wherein oil from the oil seed pulp waste residue may or may not be preliminarily extracted; and 2) separating and agitating particles of the oil seed pulp waste residue during the combustion phase to inhibit their cohesion into an integrated mass while simultaneously injecting steam into the combustion chamber.

According to another aspect of the process, the process includes the steps of drying and pulverizing the oil seed pulp waste residue to ensure a moisture content of ten percent (10%) or less and a particle size of less than 2 mm.

According to another aspect of the process, the high protein organic material is one of a high protein animal excreta or a high protein animal meat processing by-product or waste. The process according to this aspect includes the following steps: obtaining a pre-processed or “as is” high protein animal excreta or high protein animal meat processing by-product or waste which is non-auto-combustible, wherein the animal excreta has a protein content ranging from about 20% to about 60% (dry weight basis) and the animal meat processing by-product or waste has a protein content ranging from about 35% to about 85%, on a dry weight basis; removing liquid and soluble components from the high protein organic material; applying heat to dry the high protein organic material to reduce its moisture content to ten percent (10%) or less by weight; grinding the high protein organic material to reduce the high protein organic material to a particle size of less than 2 mm; separating particles of the high protein organic material during a combustion phase to inhibit their cohesion into an integrated mass by spraying the particles into a combustion chamber; simultaneously injecting steam into the combustion chamber to enhance combustion characteristics of the high protein organic material in a regulatory compliant manner; and, allowing protein thermal decomposition by-products to react with nitrogen oxides (NOX) within the combustion chamber to form water (H₂O) and nitrogen (N₂).

Also provided is a process for converting hazardous compounds to less hazardous substances. The process includes the following steps: 1) providing a non-auto-combustible organic material, wherein the organic material is a high protein organic material having a protein content of about 10%, on a dry weight basis (DWB) or greater; 2) optionally mechanically removing liquid and soluble components from the high protein organic material; 3) optionally applying heat to dry the organic material to reduce its moisture content to ten percent (10%) or less by weight; 4) pulverizing the high protein organic material to reduce the high protein organic material to a particle size of less than 2 mm, wherein the pre-combustion steps of 2) optionally mechanically removing liquid and soluble components from the high protein organic material, 3) optionally applying heat to dry the organic material to reduce its moisture content to ten percent (10%) or less by weight and, 4) pulverizing the high protein organic material to reduce the high protein organic material to a particle size of less than 2 mm, wherein the above mentioned pre-combustion steps may occur in any order; 5) separating particles of the high protein organic material during a combustion phase to inhibit their cohesion into an integrated mass by spraying the particles into a combustion chamber; 6) simultaneously injecting steam into the combustion chamber to enhance combustion characteristics of the high protein organic material; 7) allowing protein thermal decomposition by-products to react with nitrogen oxides (NOX) within the combustion chamber to form water (H₂O) and nitrogen (N₂); wherein nitrogen oxide (NOX) production ranges from about 100 parts per million (ppm) to about or greater than 300 parts per million (ppm); wherein protein thermal decomposition by-products remaining after combustion include ammonium, nitrogenous hydrocarbons, carbon monoxide (CO), carbon dioxide (CO₂), nitrogen oxides (NOX), nitrogen free radicals, nitrogen cations and other non-nitrogen containing free radical intermediate combustion reactants in the combustion gasses; 8) controlling protein thermal decomposition by-products including nitrogen oxide (NOX) production, produced during combustion within the combustion chamber; and 9) incinerating polyfluro impurities present within the processed non-autocombustible high protein organic material in the combustion chamber and/or adding and incinerating polyfluoro compounds within the combustion chamber, wherein the protein thermal decomposition by-products functions as a reactive species to incinerate polyfluoro compounds to degrade hazardous polyfluoro compounds into less hazardous substances.

According to another aspect of the process, protein decomposition by-product ash resulting from the combustion of high protein organic materials contains about 300 ppm or more ammonium, nitrogenous hydrocarbons, carbon monoxide (CO), carbon dioxide (CO₂), nitrogen oxides (NOX), nitrogen free radicals, nitrogen cations and other non-nitrogen containing free radical intermediate combustion reactants.

According to another aspect of the process, pulverizing, pressing, applying heat to dry the high protein organic material particles, spraying particles into the combustion chamber and injecting steam into the combustion chamber degrades the proteins contained within the particles and denatures them by allowing nitrogen cross-linking and other cross-linking reactions to occur within the particles, allowing the particles to complete all of the cross-linking ability before the particles contact other particles.

According to another aspect of the process, cross-linking of the high protein organic material particles is prevented by prematurely initiating cross-linking reactions of the nitrogen bonds and other cross linking reactions while the particles are being agitated and wherein the high protein organic material particles no longer adhere to each other, thereby arresting the particles tendency to adhere to each other within the combustion chamber via nitrogen bond cross-linkage and other cross-linkage reactions.

According to another aspect of the process, the step of separating the high protein organic material by spraying the processed high protein organic material into the combustion chamber is effected through use of a pneumatic stoker.

According to another aspect of the process, spraying the particles of the high protein organic material into the combustion chamber by the pneumatic stoker keeps the particles separated in the combustion chamber long enough to allow heat transfer provided by the combustion process to quickly dry and then degrade proteins present within the high protein organic material and to prevent nitrogen cross linking and other cross linking reactions between the particles that would have the particles adhere to each other.

According to another aspect of the process, the particles of the high protein organic material are separated and dispersed within the combustion chamber and ignited and burned while in suspension and separated from each other before they land and adhere to each other.

According to another aspect of the process, the non-auto-combustible high protein organic material is rendered combustible without the addition of other combustible fuels or additives.

According to another aspect of the process, the polyfluoro compound impurities and polyfluro compounds comprise polyfluoroalkyl compounds and perfluoralkyl compounds (PFAS), organic fluoride (organo fluorine) compounds and non-organic mineralized organo fluorine compounds.

According to another aspect of the process, the PFAS substances further comprise perfluorooctanoic acid (PFOA) and perfluorooctane sulfonate (PFOS).

According to another aspect of the process, the process includes controlling the concentration of ammonium, nitrogenous hydrocarbons, carbon monoxide (CO), carbon dioxide (CO₂), nitrogen oxides (NOX), nitrogen cations, nitrogen free radicals and other non-nitrogen containing free radical intermediate combustion reactants in the combustion gasses within the combustion chamber.

According to another aspect of the process, the concentration of protein thermal decomposition by-products and excess water within the combustion chamber is controlled to react and convert carbon-fluoride bonds in PFAS compounds to nitrogen, carbon dioxide/carbon monoxide, hydrogen fluoride (HF) and various inorganic fluoride containing salts and/or minerals based upon cations present in the fuel.

According to another aspect of the process, the incineration of PFAS compounds within the combustion chamber occurs at a temperature of 999° C. or below.

According to another aspect of the process, the incineration of PFAS compounds within the combustion chamber has a residence time of 1 second or less at a temperature of 999° C.

According to another aspect of the process, the nitrogen cations and concentrations of nitrogen cations present within the combustion chamber after combustion of the high protein organic material vary upon the type of high protein fuel used for combustion and ash resulting from the combustion process.

According to another aspect of the process, the ash comprises one or more of calcium, sodium, potassium, phosphorus, silica, and manganese.

According to another aspect of the process, the PFAS substances are degraded to an inorganic mineralized form.

According to another aspect of the process, the PFAS substances are degraded to one or more of calcium fluoride (CaF₂), hydrogen fluoride (HF), silicon tetrafluoride (SiF₄ aluminum fluoride AlF₃ titanium (III) trifluoride (TiF₃), titanium (IV) tetrafluoride (TiF₄), iron (III) fluoride (FeF₃), magnesium fluoride (MgF₂), potassium fluoride (KF), sodium fluoride (NaF) sulfur hexafluoride (SiF₆), sulfur decafluoride (S₂F₁₀), sulfur tetrafluoride (SF₄), sulfur difluoride (SF₂), disulfur difluoride (S₂F₂), disulfur tetrafluoride (S₂F₄), phosphorus trifluoride (PF₃), phosphorus pentafluoride (PF₅), diphosphorus tetrafluoride (P₂F₄), strontium (II) fluoride (SrF₂), barium fluoride (BaF₂), manganese (II) fluoride (MnF₂), manganese (III) fluoride (MnF₃), manganese (IV) fluoride (MnF₄), fluorapatite (Ca₅FO₁₂P₃), acuminite (SrAlF₄(OH).(H₂O)), artroeite (PbAlF_(3(OH))2), baraite (ammonium fluorosilicate) (NH₄)₂SiF₆, bultfonteinite (Ca₂SiO₂)F₄, creedite (Ca₂SiO₂F₄), cryolite (Na₃AlF₆), fluorocaphite (Ca, Sr, Ce, Na)₅(PO₄)₃F, kogarkoite (Na₃SO₄F), neighborite (NaMgF₃), sonolite (Mn₉(SiO₄)₄F₂, thomsenolite (NaCaAlF₆.H₂O), Wagnerite (Mg, Fe)₂PO₄F), zharchikhite (AlF(OH)₂, zinc fluoride (ZnF₂), beryllium fluoride (BeF₂), lithium fluoride (LiF), rubidium fluoride (RbF), cesium fluoride (CsF), radium fluoride (RaF₂), zirconium (IV) fluoride (ZrF₄) mercury (II) fluoride (HgF₂), silver (I) fluoride (AgF), copper (II) fluoride (CuF₂), nickel (II) fluoride (NiF₂), chromium (II) fluoride (CrF₂), chromium (III) fluoride (CrF₃), cobalt (II) fluoride (CoF₂), vanadium (III) fluoride (VF₃), vanadium (IV) fluoride (VF₄), scandium (III) fluoride (ScF₃), boron trifluoride (BF₃), gallium (III) fluoride (GaF₃), platinum tetrafluoride (PtF₄), cadmium fluoride (CdF₂), molybdenum (IV) fluoride (MoF₄), molybdenum (V) fluoride (MoF₅), molybdenum (III) fluoride (MoF₃), tantalum (V) fluoride (TaF₅), palladium (II) fluoride (PdF₂), palladium (II, IV) fluoride (PdF₃), gold (III) fluoride (AuF₃), tin (II) fluoride (SnF₂), tin (IV) fluoride (SnF₄), lead tetrafluoride (PbF₄), bismuth (III) fluoride (BiF₃), and cerium (III) trifluoride (CeF₃).

According to another aspect of the process, the high protein organic material is a biological waste or by-product material, wherein the biological waste or by-product material originates from waste water treatment activated sludge waste and wherein the process comprises the following order of steps: 1) providing a biological waste material or by-product comprising a waste water treatment activated sludge having a protein content of about 10% or greater, on a dry weight basis (DWB); 2) removing water, moisture and other soluble components from the biological waste material or by-product; 3) drying the biological waste material or by-product to reduce the moisture content to 10% or less by weight; 4) pulverizing the biological waste material to reduce the particle size to be less than 2 mm; 5) separating particles of the biological waste material or by-product during the combustion phase to inhibit their cohesion into an integrated mass by spraying the particles into the combustion chamber; 6) simultaneously injecting steam into the combustion chamber, wherein steam is injected to modify and control combustion reactions by reacting with nitrogen within proteins to form intermediate nitrogenous-based protein thermal combustion products which help to maintain regulatory compliance of combustion emissions; 7) controlling protein thermal decomposition by-products including nitrogen oxide (NOX) production, produced during combustion within the combustion chamber, wherein the protein thermal decomposition by-products functions as a reactive species to incinerate PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds; 8) optionally, adding additional PFAS substances in the combustion chamber for further combustion; and 9) incinerating PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds within the combustion chamber, wherein the biological waste or by-product material contains PFAS, organic fluoride (organo fluorine) compounds and/or non-organic mineralized fluorine compounds and/or wherein PFAS, organic fluoride (organo fluorine) compounds and/or non-organic mineralized fluorine compounds are added to the biological waste or by-product material within the combustion chamber for incineration.

According to another aspect of the process, the high protein organic material is hops residue and wherein the process includes the following steps in the following order: 1) extracting oils and other compounds from the ground hops utilizing mechanical separation techniques or CO₂ extraction to obtain a high protein hops waste residue having a protein content of about 25 to about 30 weight percent, on a dry weight basis (DWB); 2) providing the hops waste residue; 3) drying the hops waste residue, wherein the step of drying the hops waste residue comprises the application of heat; 4) grinding the hops waste residue into a powder by pulverizing the hops waste residue to ensure that particles of the hops waste residue have a particle size of less than 2 mm, wherein the step of pulverizing the hops waste residue includes subjecting the hops residue to a mill; 5) agitating the hops waste residue during a combustion phase to separate particles of the hops waste residue by spraying the particles into the combustion chamber to inhibit their cohesion into an integrated mass; 6) simultaneously injecting steam into the combustion chamber to enhance the combustibility of the high protein organic material; 7) controlling protein thermal decomposition by-products, including nitrogen oxide (NOX) production, produced during combustion within the combustion chamber, wherein the protein thermal decomposition by-products functions as a reactive species to incinerate PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds; 8) optionally, adding additional PFAS substances in the combustion chamber for further combustion; and 9) incinerating PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds within the combustion chamber, wherein the biological waste or by-product material contains PFAS, organic fluoride (organo fluorine) compounds and/or non-organic mineralized fluorine compounds and/or wherein PFAS, organic fluoride (organo fluorine) compounds and/or non-organic mineralized fluorine compounds are added to the biological waste or by-product material within the combustion chamber for incineration.

According to another aspect of the process, the high protein organic material is a high protein waste or meal from an agricultural source of oil production, waste by-products and by-products from an oil seed pulp processing.

According to another aspect of the process, the high protein organic material is an oil seed pulp waste residue, wherein the process includes the following order of steps: 1) obtaining an extracted high protein oil seed pulp waste residue having a protein content of about 35%, on a dry weight basis (DWB), a moisture content of ten percent (10%) or less and a particle size less than 2 mm, wherein oil from the oil seed pulp waste residue may or may not be preliminarily extracted; 2) separating and agitating particles of the oil seed pulp waste residue during the combustion phase to inhibit their cohesion into an integrated mass while simultaneously injecting steam into the combustion chamber; 3) controlling protein thermal decomposition by-products including nitrogen oxide (NOX) production, produced during combustion within the combustion chamber, wherein the protein thermal decomposition by-products functions as a reactive species to incinerate PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds; 4) optionally, adding additional PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds in the combustion chamber for further combustion; and 5) incinerating PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds within the combustion chamber, wherein the oil seed pulp waste residue contains PFAS, organic fluoride (organo fluorine) compounds and/or non-organic mineralized fluorine compounds.

According to another aspect of the process, the high protein organic material is one of a high protein animal excreta or a high protein animal meat processing by-product or waste and wherein the process includes obtaining a pre-processed or “as is” high protein animal excreta or high protein animal meat processing by-product or waste which is non-auto-combustible, wherein the animal excreta has a protein content ranging from about 20% to about 60%, on a dry weight basis (DWB) and the animal meat processing by-product or waste has a protein content ranging from about 35% to about 85% dry weight basis.

Also provided is a process for converting hazardous compounds to less hazardous substances within a traditional combustion chamber. Traditional combustion chambers include any combustion chamber having a fuel intake, an exhaust, and an ignition source known to those of ordinary skill in the art. Traditional combustion chambers include conventional chambers used in various industries including but not limited to combustions chambers used to provide heat for various industrial processes and combustion chambers used for external and internal combustion engines. The process includes the following steps: 1) providing an auto-combustible organic fuel; 2) providing a non-auto-combustible organic material, wherein the organic material is a high protein organic material having a protein content of about 10%, on a dry weight basis (DWB) or greater; 3) optionally mechanically removing liquid and soluble components from the high protein organic material; 4) optionally applying heat to dry the organic material to reduce its moisture content to ten percent (10%) or less by weight; 5) pulverizing the high protein organic material to reduce the high protein organic material to a particle size of less than 2 mm, wherein the pre-combustion steps of 3) optionally mechanically removing liquid and soluble components from the high protein organic material, 4) optionally applying heat to dry the organic material to reduce its moisture content to ten percent (10%) or less by weight and, 5) pulverizing the high protein organic material to reduce the high protein organic material to a particle size of less than 2 mm may occur in any order; 6) injecting the auto-combustible organic material into a combustion chamber; 7) spraying the non-auto-combustible high protein organic material into the combustion chamber through use of a pneumatic stoker to separate particles of the high protein organic material and inhibit their cohesion into an integrated mass during combustion; 8) simultaneously injecting steam into the combustion chamber to enhance combustion characteristics of the high protein organic material; 9) allowing protein thermal decomposition by-products to react with nitrogen oxides (NOX) within the combustion chamber to form water (H₂O) and nitrogen (N₂), wherein nitrogen oxide (NOX) production ranges from about 100 parts per million (ppm) to greater than 300 parts per million (ppm) (or alternatively from about 100 parts per million (ppm) to about 150 parts per million (ppm)), wherein protein thermal decomposition by-products remaining after combustion include ammonium, nitrogenous hydrocarbons, carbon monoxide (CO), carbon dioxide (CO₂), nitrogen oxides (NOX), nitrogen free radicals, nitrogen cations and other non-nitrogen containing free radical intermediate combustion reactants in the combustion gasses; 10) controlling protein thermal decomposition by-products including nitrogen oxide (NOX) production, produced during combustion within the combustion chamber; and 11) incinerating polyfluoro compound impurities present within the processed non-autocombustible high protein organic material in the combustion chamber and adding and incinerating additional polyfluoro compounds within the combustion chamber as an additional or alternative step, wherein the protein thermal decomposition by-products functions as a reactive species to incinerate polyfluoro compounds to degrade hazardous polyfluoro compounds into less hazardous substances.

SUMMARY OF THE DRAWINGS

Other objects and advantages of the present disclosure will become apparent from the following detailed description taken in conjunction within the attached drawings, as shown within FIGS. 1-3, which include three schematic flow diagrams of the process of the present disclosure.

DETAILED DESCRIPTION

The present disclosure provides a novel fuel product made from a high protein non-auto-combustible organic material. Examples of non-auto-combustible organic materials which may be used as a fuel source include spent grain, hops residues, solid animal waste, biological waste materials including bio-solid waste originating from waste water treatment plant bio-solid sludge waste oil seed pulp meal, distillers grains, feather meal (a by-product of the poultry industry), high protein animal meat processing by-product (e.g., meat and bone meal, feathers, feather meal, and animal excreta) and other high protein organic materials as a fuel sources that are processed to change its composition, structure, handling and combustion environment in order to sufficiently increase its combustibility. In certain aspects of the process, these changes in composition, structure, handling, and combustion environment allow the high protein non-auto-combustible waste material to be used as a primary or sole fuel product in accordance with air quality standards and other environmental regulations and law.

The high protein waste materials mentioned above may be categorized into the following four general types of waste materials: 1) bio-solids from waste water treatment plants (containing from 10% protein to 30% protein on a dry weight basis); 2) high protein fermentation waste and waste by-products (examples include but are not limited to spent grain, hop residue, yeast and protein precipitates) (containing from 20% protein to 50% protein on a dry weight basis); 3) high protein waste and by-products from agricultural sources of oil production and seed processing, waste by-products and by-products (examples include but are not limited to sources of oil seed pulp meal (also called seed meal) including cotton seed pulp (or cotton seed meal), sunflower seed pulp (or sunflower meal), soybean pulp and hulls, olive pulp, coconut pulp, cotton seed, canola oil, vegetable oil in general, wheat middlings, corn gluten mill feed, hominy feed and combinations thereof) (containing from 30% protein to 50% protein on a dry weight basis); and 4) high protein animal meat processing by-product (examples include but are not limited to meat and bone meal, feathers, feather meal and animal excreta) (containing from 35% protein to over 80% protein on a dry weight basis).

Sources of spent grains, distillers grains and hops residues include breweries, distilleries and ethanol production facilities. High protein waste products made from grain (e.g., spent grain) hops residues and distillers grains are a by-product of a brewing process. In one form of the present disclosure, a high protein fermentation waste from spent grain is obtained primarily as a malt by-product of a beer brewing process which is processed to yield a high protein organic material which may be used as a fuel. A summary of this process is shown for illustrative purposes within FIG. 1 which for exemplary purposes describes the processing of spent grain into a combustible fuel, although various aspects of the process illustrated within FIG. 1 and described herein may also be applicable to processing other high protein organic materials into a combustible fuel. During brewing, the grain is first crushed or pulverized by a hammer mill 10 to reduce it to a finely ground median particle size generally less than 2 mm. In other aspects of the present teaching, the grain may be reduced to a median particle size of 0.25 mm to 0.6 mm with less than 1% of the grain being greater than 2 mm, however, this reduction in particle size is not necessary for combustion to occur as a higher protein content generally implies an improved combustion process for smaller particle sizes. The median, particle size between 0.25 mm to 0.6 mm means that fifty percent (50%) of the grain particle mass is greater than and fifty percent (50%) of grain particle mass is smaller than the median size. Pulverizing the grain reduces adhesion among various elements of the grain which normally serves to solidify the grain into one cohesive and air-impermeable mass upon combustion. It also increases the surface area of the particles to facilitate the reduction of moisture and increase combustibility. In one form of the present disclosure, the mill used in this instance is a Meura ClassicMill CLM3 model fine grinding hammer mill with horizontal shaft. This grinding process to obtain the desired particle size, for combustion, can be accomplished before or after the brewing and drying process, prior to combustion. Although the Meura ClassicMill CLM3 mill model is mentioned above, any other suitable device known to those of ordinary skill in the art may be used to pulverize the grain.

After pulverizing, the grain is moved such as by a drag chain conveyor to a mash vessel 12 and hydrated from which it may optionally be moved such as by a centrifugal pump to a mash filter press 14 where it is pressed. This step removes water mechanically from the grain material which increases the overall thermal efficiency of the process and allows excess heat to be available for other uses within the process. For example, heat vaporization of excess water wastes the application of heat energy which might be redirected for other beneficial uses such as steam generation for industrial use.

The latter process steps reduce the moisture content and removes soluble sugar and protein contents which also act as adhesives during subsequent drying of the spent grain. In certain aspects of the present teaching, the moisture content is reduced to below 65%. With these compounds reduced, the tendency of the grain particles to establish cohesion and structural integrity during subsequent drying and burning as a fuel is significantly reduced. The fact that the spent grain has been pulverized, also enables the cloth to act as a filter through which the moisture passes when the spent grain is pressed on the cloth. The latter also reduces the energy needed to further dry the spent grains before its use as fuel. In one preferred process of the present disclosure, a Meura 2001 mash filter press available in the industry may be used. However, other methods and devices may also be used to press the moisture and other soluble compounds from the spent grain as described above. Due to the compression of the spent grains to remove moisture, it is preferred that air pulses be directed into the spent grain on the filter cloth before opening the filter to help break up the spent grain cake to facilitate release of the spent grain from binding to the filter cloth when the filter is opened. The spent grain is then moved to a hopper 16 by a pneumatic pump from which it is moved to a grain drying drum 18 by an auger and pulled through the drier drum by a pneumatic fan, for example.

The next step in the process is that the spent grain is dried to further reduce the moisture content to ten percent (10%) by weight or less. In one embodiment, a rotating dryer drum 18 is used to receive the spent grain and is rotated while heated air in the drum subjects the spent grain to the desired drying temperature while the drum is rotating. The reduced finely ground spent grain particles helps speed up the drying process to reach the desired moisture level preferably ten percent (10%) or less by weight in order to increase its combustibility. A suitable dryer drum that can be used is one made by Baker Rullman which is readily available on the market. Other methods of drying the spent grain to sufficiently reduce its moisture content may of course be used. Also, grinding the dried spent grain can be done after the drying process to achieve the desired particle size distribution.

After having been processed as described above, the spent grain can be stored in a hopper 20 for immediate or eventual use as a primary fuel source. For example, the spent grain may be introduced in a boiler 22 used in a brewery to produce steam for heating the brew house vessels. In the embodiment shown in FIG. 1, the dried spent grain is moved to the hopper 20 by a cyclone 24. An auger is then used to convey the spent grain fuel into the combustion chamber 28. For combustion within the boiler 22 (e.g., a steam boiler), the spent grain is moved in any suitable manner, from the fuel bin through the combustion chamber 28, such as down an inclined grate 26 positioned within the combustion chamber 28 while the grate 26 is agitated or vibrated. In one process, a motor 30 connected by linkage 32 to the grate 26 is employed to vibrate the grate as the spent grain is moved through the combustion chamber 28. In another process, illustrated within FIG. 2, steam is injected into the combustion chamber 28 from a steam generator 40 during the combustion process. The timing frequency and intensity of the inclined grate agitation can be controlled and adjusted as needed for best combustion. The angle of the inclined grate being combined with the agitation or vibration of the grate helps to keep the spent grain moving through the combustion chamber while it burns to inhibit cohesion and solidification of its particles. Under normal circumstances, spent grain that has not been processed as described above tends to form a sponge-like impermeable, cohesive mass when heated which inhibits the transfer of oxygen and heat to the interior of the mass and thereby prevents sufficient combustion and generates large amounts of smoke while also causing an excessive buildup of material within the combustion chamber. In contrast, the process of the present disclosure not only sufficiently reduces the moisture content and particle size of the spent grain, soluble proteins and sugars which act as binding agents during heating, but it also, through agitation and separation, breaks up the nitrogen bond cross linking and other cross-linking reactions (for example, non-nitrogen based cross-linking such as cross linking of soluble sugars during sugar decomposition) that occurs during thermal degradation of protein, all of which can inhibit combustion. In addition, the vibration and continual movement of the spent grain through the combustion chamber further breaks up the spent grain into smaller clumps thereby avoiding cohesion of the particles into an, agglomerated cohesive mass. This agglomeration of particles prevents sufficient heat transfer and diffusion characteristics for oxygen and water with the nitrogenous hydrocarbon combustion reactions of the agglomerated protein mass. In one process of the present disclosure, a King Coal combustion chamber may be used. After combustion, waste ash is collected and disposed of. The process of the present disclosure provides effective combustion of the spent grain to allow it to be used as the sole source of fuel, that is, without the need for combining it with a readily combustible fuel source such as wood, wood chips, wood by-products, fuel oil, natural gas, coal or other combustibles or additives to aid in combustion.

In another process of the present disclosure, rather than separating the spent grain particles during combustion by vibrating or agitating the particles through means of the grate 26, linkage 32 and motor 30 as described above, the spent grain particles are separated and disbursed during combustion by being introduced or fed and sprayed into the combustion chamber by a device such as a pneumatic stoker. In one embodiment, as shown in FIG. 2, a pneumatic stoker 34 is connected to the combustion chamber 28 by a linkage 32 to blow the spent grain through the combustion chamber 28. The pneumatic stoker sprays the spent grain particles or particles of another type of high protein organic material into the combustion chamber thereby separating and disbursing the particles. The particles are ignited and burned while they are in suspension and separated from each other and before they can come into contact with and adhere to each other on the grate, bed, other surface or while suspended. This method also increases heat transfer to fully dehydrate the particles which needs to happen for protein denaturing to fully occur and increases the oxygen flow for combustion to allow the spent grain to be used as the sole fuel source in brewery boilers. In another process disclosed herein, steam is simultaneously injected into the combustion chamber 28 from a steam generator 40 during as the organic particulate material is sprayed within the combustion chamber by the pneumatic stoker.

The above-described process steps reflect the order of steps for processing a spent grain fuel product for combustion as disclosed herein. However, in the case of other fuels, the order of steps for processing the fuel for combustion may differ. For example, in some cases, the step of mechanically removing moisture and other soluble components from the fuel material as described in step 2 may be entirely eliminated.

As previously mentioned, the steps described above may generally be applied to other non-auto-combustible high protein organic materials. These other high protein organic materials include other high protein fermentation by-product materials such as distillers grains, yeast and hops residues, bio-solid waste materials from waste water treatment plants, oil seed pulp (often called seed meal), animal excreta, and high protein meat production waste (including meat and bone meal, feathers, feather meal and animal excreta) and other high protein wastes. The waste materials provided herein may also be described as biological waste materials or organic materials or biological materials or as by-products. As is the case for spent grain, these high protein organic materials present combustion challenges which are difficult to overcome due to their respective high protein content. High protein organic materials that are traditionally considered as non-auto-combustible materials which may be used in a process for making a combustible fuel product typically have a protein content of about 10% or greater, on a dry weight basis (DWB) and are ordinarily considered insoluble. In other cases, high protein non-auto-combustible organic materials used for making a combustible fuel product have a protein content of about 20% or greater. High protein fermentation waste and waste by-products processed into a fuel product have a protein content ranging from about 25% to about 40%, on a dry weight basis (DWB). For example, hops residues through processing or concentrating of hops alpha/beta acids and hops oils has a protein content of about 25 to about 30%, on a dry weight basis (DWB). Bio-solids from waste water treatment plants have a protein content ranging from about 10% or greater, on a dry weight basis (DWB) and in some cases from about 20% or greater, on a dry weight basis (DWB). Animal excreta has a protein content ranging from about 20% to about 50% or more, on a dry weight basis (DWB). For example, municipal waste water treatment activated sludge and animal excreta processed into a fuel product can have a large protein content range of about 10% (DWB) to about 60% (DWB) depending upon the specific plant operations. High protein waste from agricultural sources of oil production processed into a fuel product has a protein content ranging from about 20% to about 50%, on a dry weight basis (DWB). For example, the general class of an oil seed pulp meal (e.g., including but not limited to sunflower or rape seed, soy bean, corn, cotton seed, coconut, olive oil, etc.) fuel product has a protein content of about 35%, on a dry weight basis (DWB). Distillers Dried Grains are similar to brewers dried grains but from a distillery also has a protein content of about 30%, on a dry weight basis (DWB). High protein meat production waste and waste by-products processed into a fuel product have a protein content ranging from about 30% to about 85%, on a dry weight basis (DWB). For example, feather waste fuel product has a protein content of about 80% to about 85%. All of these materials are characterized as high protein by-products or waste materials which could be used as fuel products. In each of these alternative fuel types, the degree of hydration and the degree of pulverizing to achieve the appropriate particle size distribution for combustion is dependent upon the respective particles' adhesion characteristics and the protein content which is directly proportional to the nitrogen cross-linking capability at the molecular level. For example, during thermal degradation, the nitrogen bonds in proteins cross link in a macro mechanical way which results in clumping, crusting or clinkering of the fuel product. This restricts oxygen transmission, heat transfer and the diffusion of reaction compounds such as steam into the burning fuel. The low moisture content obtained by process step 3) and the small particle size obtained by process step 1) affects how quickly the temperature of the particle is raised. The process of quickly driving off the moisture and subsequently heating the particles degrades the proteins, denaturing them by essentially having the nitrogen bonds and other cross linking reactions react to complete all of their cross-linking ability on the surface of the particles if not all through the particles while they are agitated in suspension before the particles can touch other particles. Once the cross linking is complete, the particles will no longer adhere to each other. This arrests the particles tendency to adhere to each other via a nitrogen bond cross linkage and through other cross linking reactions. The small particle size obtained from step 1) and the agitation and/or separation applied during step 4) keep the surface to oxygen and injected steam (water vapor) exposure appropriate for oxygen diffusion enabling complete appropriate combustion to be accomplished and for the injected steam (water vapor) to more effectively react with the nitrogen in protein. Steps 1) and 4) work in conjunction to produce a combustible fuel product. For instance, if the small particles were allowed to easily touch during protein thermal degradation, they would form larger clumps that would be glazed over with a cross linked protein layer reducing oxygen and steam diffusion necessary for regulatory compliant emissions during combustion. On the other hand, if the particles were too large to begin with, this would reduce the oxygen availability or diffusion necessary for complete combustion to occur as protein would cross link glazing over the larger particles reducing oxygen and steam (water vapor) diffusion necessary for regulatory compliant emissions during combustion.

Regulatory compliant emissions, are intended to encompass any set of standards established by any governmental regulatory agency to protect the environment. For example, in the U.S., emissions are in certain situations regulated to not exceed 20% opacity averaged over 6 minutes. The combustion process disclosed herein is capable of meeting this regulatory standard as well as other standards set by other agencies and governments of other countries including standards which are more stringent. For example, the combustion process disclosed herein is capable of meeting opacity requirements within time intervals shorter than six minutes, lower opacity levels averaged over 6 minutes, and is also capable of meeting regulations which require specific limits or amounts (e.g., pounds of NOX emissions). The present process can also achieve even lower limits than that which is currently required in the U.S.

As mentioned above, in the case of other high protein organic materials processed to become fuels, the order of steps for processing the fuel for combustion may differ and in some cases, the step of mechanically removing moisture and other soluble components from the fuel material as described in step 2) may be eliminated. For example, in one embodiment, the pulverizing step (i.e., step 1) above) and the drying step (i.e., step 3) above) may need occur in a different order to ensure that fine particles do not re-adhere together during the drying process right before they are fed into the combustion chamber.

To make a fuel product from hops residue, the hops must be processed to extract out oils and desirable compounds. The processing of hops to extract the oils and other desirable compounds leaves a high protein residue. In order to process the hops, a hops processor first dries the hops to obtain dry hops cones. Next, the dry hops cones are ground. Then, the hops is subjected to an extraction such as a CO₂ extraction or other mechanical separation technique known within the art to remove or concentrate the essential oils and other desirable compounds. Various types of extraction methods may be used in this process including but not limited to normal CO₂ extraction processes, CO₂ triple point extraction processes as well as other mechanical separation techniques suitable for use within the art. The separation and/or extraction process allows the desirable compounds to be removed or extracted from the hops, creating a by-product or hops residue waste material. In certain cases, after the waste or hops residue is removed or extracted, it may need to be re-ground. In some embodiments, the hops residue is dried and pre-ground but due to processing may reform into larger particle groupings that will need to be re-ground to a powder. After processing the hops residue for combustion, the hops residue may be agitated and/or separated as described above during the combustion phase to separate particles of the fuel product to inhibit their cohesion into an integrated mass. In certain embodiments, the separation step during the combustion phase is accomplished through the use of a pneumatic stoker. In other embodiments, the agitation step during the combustion phase is accomplished through the use of a vibrating grate. As described above, the process steps for making a fuel product from hops residue may occur in any order.

To make a fuel product from biological waste material, one can process municipal waste water treatment activated sludge waste, which is a human bio-hazard which may contain PFAS and other fluorinated compounds (also referred to herein as polyfluoro impurities and polyfluoro compounds) and which may originate from industrial sources or fire safety control sources. Waste water sludge which contain polyfluoro compounds such as PFAS cannot be used to make compost or otherwise treated and used for land applications. Sources of polyfluoro compounds such as PFAS that have contaminated waste water sludge require the waste water sludge to be treated differently such that the waste water sludge can no longer be treated in a combustion process unless the combustion process also contemplates degrading PFAS and other fluorinated compounds. Rather, the combustion process must meet the standards required for combusting and degrading polyfluoro compounds, in particular, PFAS. The process encompasses controlling protein thermal decomposition by-products including ammonium, nitrogenous hydrocarbons, carbon monoxide (CO), carbon dioxide (CO₂), nitrogen oxides (NOX), nitrogen cations, nitrogen free radicals and other non-nitrogen containing free radical intermediate combustion reactants in the combustion gasses for further combustion with hydrogen fluoride and inorganic fluorine compounds, i.e., fluoride mineralized in the form of salts within the ash before such by-products are discharged into air. The process begins with the biological waste material starting off very wet (approximately 99% water). This first step is therefore to dewater the biological waste material as much as possible using flocking agents, centrifuges and dewatering separators. The biological waste material will then be dried typically on a heated rotating drum, a heat progressing filter belt, drum filter or other suitable drier. This results in dry flakes or pellets having less than 10% moisture which are too large and which will need to be pulverized. Thus, the processing of biological waste material into a fuel product requires the following steps: 1) mechanical removal of water, moisture and other soluble components from the biological waste material; 2) drying the biological waste material to reduce the moisture content to 10% or less by weight; 3) pulverizing the biological waste material to reduce the particle size to be less than 2 mm; and 4) agitating and/or separating the biological waste material as described above during the combustion phase to separate particles of the biological waste material to inhibit their cohesion into an integrated mass and 5) simultaneously injecting steam within the combustion chamber. The combustion process may occur within an integrated steam boiler, an incinerator, furnace or any other type of combustion chamber typically used by those of skill in the art to generate heat. In certain embodiments, the separation during the combustion phase is accomplished through the use of a pneumatic stoker. In other embodiments, the agitation step during the combustion phase is accomplished through the use of a vibrating grate or a combination of both a pneumatic stoker and a vibrating grate. It is noted that step 2) uses any means within the purview of an individual of suitable skill in the art to remove free water. Also; the high water content of the biological waste material requires the application of additional heat to the waste material in the drying step. In general, municipalities have an interest in applying the disclosed process not only for heat generation but more importantly, in order to dispose of bio-hazardous material via combustion. In addition, the dried waste product has a higher value as fuel than as other means of disposal. For example, use of land application for disposing biological waste material (if regulations allow) has a much lower revenue value to a municipality than the value that would be Obtained if the biological waste material were to be used as a fuel for the production of heat.

To make a fuel product from animal excreta; one can process the animal excreta in a manner similar to the process steps described above with respect to biological waste material. Animal excreta, is a bio-hazard which also starts off very wet. This fecal material is first dewatered using thickeners, flocking agents, presses, centrifuges and dewatering separators to separate out the settable solids. Next, the settable solids are dried on commonly available industrial drying equipment such as a belt or drum drier. The resulting dry flakes or pellets are then pulverized. Thus, the processing of animal excreta into a fuel product requires the following steps: 1) mechanical removal of water, moisture and other soluble components from the animal excreta; 2) drying the animal excreta to reduce the moisture content to 10% or less by weight; 3) pulverizing the animal excreta to reduce the particle size to be less than 2 mm; and 4) agitating and/or separating the animal excreta as described above during the combustion phase to separate particles of the animal excreta to inhibit their cohesion into an integrated mass and 5) simultaneously injecting steam within the combustion chamber to assist in the combustion reactions and to maintain regulatory compliant combustion based upon the exact nature of the organic materials. In certain embodiments, the separation step during the combustion phase is accomplished through the use of a pneumatic stoker. In other embodiments, the agitation step during the combustion phase is accomplished through the use of a vibrating grate. It is noted that step 2) uses any means within the purview of an individual of suitable skill in the art to remove free water. Also, the high water content of the biological waste material requires the application of additional heat to the waste material in the drying step. This process may be applied by farms to not only generate some form of heat recovery but as importantly, to dispose of a bio-hazardous material rather than holding it until growing season for land application as fertilizer (farms hold this material for up to a full year). The benefit of employing this process is that the value of the waste stream as an energy source is much more significant than its value as a soil enhancement. Additional benefits of employing this process include reducing foul odor and reducing the liability for having exposed standing waste ponds which are regulated stringently by the regulatory agencies.

Oil seed pulp meal streams have a fairly high heating value. To make a fuel product from a high protein waste from an agricultural source of oil production such as oil seed pulp meal, the oil seed pulp meal undergoes a seed oil extraction. In the extraction process, high protein residue is separated from the oil and the pulp waste material (often called seed meal which maybe already dry (shelf stable)) and ground ready for animal feed processing. Additional drying and pulverizing steps may be applied to the oil seed pulp meal material as described above as deemed necessary. For example, in certain embodiments, the oil seed pulp meal material may be dried to reduce the moisture content to 10% or less by weight and then pulverized or in reverse order to reduce the particle size to be less than 2 mm. The oil seed pulp meal material is then agitated and/or separated as described above during the combustion phase to separate particles of the oil seed pulp meal material to inhibit their cohesion into an integrated mass while simultaneously injecting steam within the combustion chamber to assist in the combustion reactions and to maintain regulatory compliant combustion based upon the exact nature of the organic materials. The grinding step may occur immediately after the extraction step or may occur after a drying and pulverizing as described above. In certain embodiments, the separation step during the combustion phase is accomplished through the use of a pneumatic stoker. In other embodiments, the agitation step during the combustion phase is accomplished through the use of a vibrating grate. The pneumatic stoker and the vibrating grate may also be used together.

To make a fuel product from a high protein fermentation waste such as distillers grains, one would follow the process described above with respect to the processing of brewery spent grains. In this regard, distillers dried grains and any grains from the fermentation industry are regarded by those of skill in the art to be similar to those of brewers dried spent grains. In addition, the process described above may also be applied to other types of high protein waste.

To make a fuel product from high protein meat production waste and waste by-products such as meat and bone meal, feathers, feather meal and excrement (animal excreta), one may process the by-products or waste material by cooking and milling to stabilize the product so that it can be made into a feed supplement. One would then follow the general process described above with respect to other high protein organic waste materials.

The numerous types of non-autocombustible high protein organic materials referenced above including high protein fermentation waste (e.g., distillers grains, yeast and hops residue), bio-solid waste material, oil seed pulp waste, animal excreta, and high protein meat production waste and waste by-products may also be used as an additive in traditional combustion chambers for the destruction of polyfluoro compounds such as PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized organo fluorine compounds.

Accordingly, the present disclosure also provides a process for converting hazardous compounds to less hazardous substances within a traditional combustion chamber. The process includes the steps 1) providing an auto-combustible organic fuel (e.g., any traditional type of fossil fuel (e.g., coal, oil or gasoline); and 2) providing a non-auto-combustible organic material as disclosed above. The organic material is a high protein organic material having a protein content of about 10%, on a dry weight basis (DWB) or greater. The process initially includes the steps of optionally, mechanically removing liquid and soluble components from the high protein organic material; optionally, applying heat to dry the organic material to reduce its moisture content to ten percent (10%) or less by weight; and pulverizing the high protein organic material to reduce the high protein organic material to a particle size of less than 2 mm. These steps, referred to as pre-combustion steps may occur in any order depending on the processing requirements of the specific non-autocombustible organic material. The auto-combustible organic material is then injected into a combustion chamber by spraying. The spraying of the non-auto-combustible high protein organic material into the combustion chamber may be accomplished through use of a pneumatic stoker and has the effect of separating particles of the high protein organic material within the combustion chamber to thereby inhibit their cohesion into an integrated mass during combustion. Simultaneously, while being sprayed into the combustion chamber, steam is injected into the combustion chamber to enhance combustion characteristics of the high protein organic material. Protein thermal decomposition by-products are subsequently allowed to react with nitrogen oxides (NOX) within the combustion chamber to form water (H₂O) and nitrogen (N₂). It is noted that nitrogen oxide (NOX) production within the combustion chamber ranges from about 100 parts per million (ppm) to greater than 300 parts per million (ppm) and that the protein thermal decomposition by-products remaining after combustion include ammonium, nitrogenous hydrocarbons, carbon monoxide (CO), carbon dioxide (CO₂), nitrogen oxides (NOX), nitrogen free radicals, nitrogen cations and other non-nitrogen containing free radical intermediate combustion reactants in the combustion gasses. The amount of protein thermal decomposition by-products produced during combustion within the combustion chamber is then controlled to provide the conditions of combustion of polyfluoro compounds. Finally, polyfluoro compound impurities present within the processed non-autocombustible high protein organic material in the combustion chamber are incinerated. Additional polyfluoro compounds may also be added within the combustion chamber for incineration as an alternative or additional step. It is noted that the protein thermal decomposition by-products functions as a reactive species to incinerate polyfluoro compounds to degrade hazardous polyfluoro compounds into less hazardous substances.

In each of the processes described above with respect to high protein bio-solids from waste water treatment plants; high protein animal excreta; high protein fermentation waste and waste by-products; high protein waste from agricultural sources of oil production, high protein waste by-products and high protein by-products; and high protein meat production waste by products and by-products, the separation step during combustion may be applied by a pneumatic stoker or by an auger which drops the grain onto a vibrating bed and transfers the fuel product to the combustion chamber through an incline or a combination of both. However, by blowing or spraying the particles into the combustion chamber, the pneumatic stoker keeps the particles separated in the combustion chamber long enough to allow the heat transfer provided by the combustion process to quickly dry the particles out and to degrade the proteins and other compounds within the combustible fuel product. This prevents nitrogen-based cross linking and other non-nitrogen based cross-linking reactions. Examples of non-nitrogen based cross linking reactions include cross linking of carbohydrates (these can include simple sugars to more complex dextrins) during thermal decomposition between the particles that would result in the particles adhering to each other. This unique feature for addressing cross linking and then also degrading proteins with steam is not considered by combustion technologists and therefore not addressed in traditional feeding mechanisms of potential non-auto combustible fuel into the combustion chamber.

As mentioned above, the combustion process provides for both quickly driving off the moisture and subsequently heating the particles to denature the proteins. Although the timing of these events occurs relatively quickly for the particles to be fully dehydrated for combustion, the process also requires the input of water into the combustion chamber in order to facilitate certain chemical combustion reactions within the combustion chamber. In short, there are four sources for introducing water within the combustion chamber. Those sources include water within the combustion air which supports the combustion process, water within the particle itself that is to be combusted, the combustion reactions which generate water and steam which is injected into the combustion chamber. By controlling the amount of water that is introduced within the combustion chamber from these four sources, the temperature of the combustion process can be controlled and combustion reactions can be influenced to maintain regulatory compliance in order to utilize otherwise non-auto-combustible high protein organic material or waste product or by-product as a fuel. Water produced during combustion is basically the result of oxidation of hydrocarbons which primarily produce carbon dioxide and water. Water is also an active part of many intermediate combustion reactions. The majority of water in traditional combustion comes from the fuel combustion reaction products and a much smaller amount which comes from the water in the fuel itself (assuming this water concentration is 10% moisture or less) and from the humidity in combustion air. In the disclosed process, a significant amount of water in the form of steam is comparable to the amount produced due to combustion is injected into the combustion chamber. In certain aspects of the present disclosure, the amount of water (i.e., steam) injected into the combustion chamber in the form of steam may be equivalent or nearly equivalent to the amount produced during normal combustion. Under certain operating conditions, by injecting a nearly stoichiometric equivalent amount of water in the form of steam, the reaction kinetics are affected to influence the balance of the products verses the reactants in the combustion reaction itself. However, in other aspects of the present disclosure, it may not be necessary to inject an equivalent, stoichiometric equivalent or nearly stoichiometric equivalent amount of water or steam within the combustion chamber to achieve the desired results as injecting such an amount of water or steam into the combustion chamber may not assist and/or may hinder combustion under certain conditions. In addition, it is also noted that the reaction of nitrogenous hydrocarbons (e.g., intermediate ammonium and other nitrogen containing compounds such as nitrogen free radicals) assists in gasifying the nitrogen from protein thermal combustion products that aids in nitrogen oxide (NOX) control.

Without steam injection, the water content in the combustion chamber could be less than 8% due to the water in the fuel, less than 15% could be from water contained in the combustion air and over 77% could be from the combustion reactions. With steam injection comparable to the combustion water source, these ratios change to less than about 4% of the water being from the fuel, less than about 8% of the water being from the combustion air, about 44% of the water being from combustion sources and about 44% of the water being from direct steam injection.

While steam is used in traditional combustion to mechanically move and manage ash transport in combustion chambers, to lower temperatures and to effect coal gas reactions (CO and CH4), the use disclosed herein is unique in its effect on the nitrogen content of the high protein organic waste materials. In particular, the combustion reactions disclosed herein are capable of controlling NOX levels compared to traditional processes applied to other readily combustible fuels.

This regulatory combustibility of traditionally non-auto-combustible waste products is achieved by influencing the temperature of the combustion which also influences the amount of NOX (Nitrogen Oxides) production during the combustion process. This is how organic fluorine compounds are converted to mineralized inorganic fluorine compounds. Through the introduction of steam within the combustion chamber, the temperature of the combustion chamber can be controlled, nitrogenous hydrocarbons compounds are reacted with water and combustion reactions can be influenced so that NOX production (elevated or non-elevated amounts) can be controlled. This provides additional agitation which also provides additional time for the particles to heat up allowing nitrogen cross-linking and other cross linking reactions within the particles to occur before ignition and combustion. Accordingly, the injection of steam within the combustion chamber allows one to control the combustion process between various types of high protein organic materials providing optimal conditions for combusting high protein organic materials that are typically not auto-combustible. This also allows for organo fluorine compounds to be degraded by mineralizing the fluorine.

In addition to injecting steam within the combustion chamber, in certain aspects of the process disclosed herein, it may be desirable to increase the protein content of the high protein organic material before it enters the combustion chamber. This may be accomplished by injecting a secondary high protein organic material such as yeast, precipitated proteins, spent hops or other high protein materials within the high protein organic material before it is pulverized (ground) and/or before it is dried. For example, the addition of yeast may be added to increase the protein content of wet spent grain before it enters the drier.

The process described above allows for the effective combustion of high protein organic materials (e.g., bio-solids from waste water treatment plants; animal excreta; high protein fermentation waste and waste by-products; high protein waste from agricultural sources of oil production waste by-products and by-products; and high protein meat production waste and waste by-products) which allows for a specific type of high protein organic material to be used as the primary sole source of fuel. While these wastes or by-products may be incinerated and burnt without undergoing the process described above, combustion can only occur when the majority of the energy comes from traditional auto-combustible fuels like wood products and wood by-products; hydrocarbons like natural gas, coal and fuel oil. The process disclosed herein eliminates any need to combine the high protein organic material with a readily combustible fuel source such as wood, wood chips, wood by-products, coal, fuel oil, natural gas, coal or other combustibles or additives to aid in combustion. The process disclosed herein further allows the high protein organic material to undergo combustion within a furnace, steam boiler, incinerator or other combustible chamber as a primary or as a sole fuel source.

The above-described process can be described in the following five steps: 1) pressing the fuel material to mechanically remove moisture and other soluble components; 2) drying the fuel material to reduce the moisture content to 10% or less by weight; 3) pulverizing the fuel material to reduce the particle size to be generally in the range less than 2 mm; 4) agitating and/or separating the fuel product during the combustion phase to separate particles of the fuel product to inhibit their cohesion into an integrated mass; and 5) injecting steam within the combustion chamber to enhance the combustibility of the spent grain and to regulate the nitrogenous hydrocarbon combustion reactions related to the organic nitrogen contained in the proteins or otherwise high protein non-combustible organic material. Although the order of steps generally follows the sequence of steps mentioned above, in certain embodiments, the pulverizing step (step 1) may occur after the drying step (step 3) but prior to combustion (step 4).

With respect to the combustion of these examples of high protein biological materials as fuel products, one might assume that these fuel products would have abnormally high NOX (Nitrogen Oxides) emissions due to the high protein and organic nitrogen content of these fuels. In fossil fuels, even a slightly elevated nitrogen content results directly in elevated NOX production. However, the present process controls nitrogen oxide formation to levels ranging from about 100 ppm to greater than 300 ppm. This is due to the relatively weak binding of nitrogen to the carbon-based proteins and its combustion reactions with excess water provided for in the present process by steam injection. In essence, the chemical path of protein thermal decomposition allows the nitrogen to take an intermediate step to form urea, ammonium compounds and even ammonia in the present process. It is noted that ammonia is sometimes injected into combustion furnaces for boilers to lower NOX production. This is represented by the following generically balanced general chemical formula: aNH₃ (ammonia)+bNOX (nitrogen oxides)=cN₂ (nitrogen)+dH₂O (water). Where a, b, c and d will vary numerically based upon the actual form that the NOX takes. The present process does not necessarily require the partial injection of ammonia into the combustion chamber due to the type of organic protein combustion reactions which occurs during the process which include the generation of nitrogenous hydrocarbons (e.g., intermediate ammonium and other nitrogen containing compounds). In any event, the presence of the weak nitrogen bonded protein generates ammonia and other nitrogenous hydrocarbon compounds formed in the present process within the combustion chamber which allows combustion of high nitrogen content fuel to be used without higher NOX production. Accordingly, the present disclosure also encompasses a process for making a combustible fuel product from a non-auto combustible high protein biological material used as an additive with injected steam for a combustion system to enable having controlled nitrogen oxide (NOX) production wherein protein thermal decomposition by-products react to mineralize fluorine from organofluorine compounds and achieve polyfluoro compound and organo fluorine compound destruction.

A general summary of the process for making a combustible fuel product from a high protein organic material that is non-auto-combustible is illustrated within FIG. 2. First the high protein organic material is crushed or pulverized by a mill 10 to reduce the material to a finely ground particle size. The term “mill” is intended to include a roller mill, a hammer mill, any type of grinder and any type of particle reduction process that a person of ordinary person of skill in the art would utilize to reduce the particle size of materials. After pulverizing, the high protein organic material is moved to a vessel 12 and subsequently moved to a filter press 14 (or any mechanical water separator) where it is pressed to mechanically remove water and other liquids from the material. It is noted that any means known to those of skill in the art may be utilized to mechanically remove water and other liquids from the material. The high protein organic material is then moved to a hopper 16 by a pneumatic pump and subsequently subjected to a drier 18 to further remove water, liquid and moisture from the material. The high protein organic material is separated from the air vapor mixture by a cyclone 24, for example, and is then moved to a hopper 20. For combustion with the boiler 22 (e.g., a steam boiler), the high protein organic material is moved in a suitable manner from the fuel bin by a spraying device such as a pneumatic stoker (34) into the combustion chamber 28. In another process, steam is injected into the combustion chamber 28 from a steam generator 40 while simultaneously spraying high protein organic material within the combustion chamber. After combustion, waste ash is collected and disposed of. The above described process illustrated within FIG. 2 for producing a combustible fuel product from a high protein organic material is intended to be a generalized description of the overall process. It is to be understood that variations, modifications and rearrangements of the components shown within FIG. 2 may be necessary such as in the case of producing a combustible fuel product from a high protein biological material from oil seed pulp meal as described within this document. For oil seed pulp meal, an extractor may be incorporated at the front end of the process to remove residue oils from the oil seed pulp meal before drying and subsequently pulverizing the oil seed pulp meal. Furthermore, because the drying and pulverizing steps may be optional with respect to oil seed pulp meal, it may not be necessary to include a mill 10 and/or a dryer 18 within the process in certain cases. It should be noted that with certain high protein organic materials, parts of the process described in FIG. 2 will not be necessary as the by-product may already be partially processed as received. For example, in the case of meat and bone meal, feathers, feather meal, oil seed pulp residue, all of these items may already be dried (pre-processed) to have or already have less than 10% moisture, eliminating the need for the Filter Press 14 and the Drier 18 (i.e., mechanical removal of moisture of these materials may not be necessary). Also, the process and order of steps described within FIG. 2 may vary depending on the type of high protein non-auto-combustible organic material that is being utilized. For example, with respect to biological waste material originating from waste water treatment sludge, it may be necessary to first subject the biological waste material to a drier to reduce the moisture content before subjecting the biological waste material to a mill 10 for pulverization.

In further embodiments, by-products obtained from the combustion of the high protein organic material fuel products obtained from the processes described above may be utilized to convert or degrade hazardous compounds to less hazardous substances. Such hazardous compounds include but are not limited to polyfluroalkyl compounds and perfluoralkyl compounds commonly referred to as PFAS. PFAS compounds may further include perfluorooctanoic acid (PFOA) and perfluorooctane sulfonate (PFOS). By-products obtained from the combustion of high protein organic material fuel products that are utilized in the conversion or degradation of such hazardous compounds include protein thermal decomposition by-products such as ammonium, nitrogenous hydrocarbons and nitrogen-based compounds including nitrogen oxides (NOX) and nitrogen free radicals. These protein thermal decomposition by-products remaining after combustion within the combustion chamber are harnessed for further combustion. In this process, polyfluoro compounds such as PFAS either present in the combustion chamber or added to the combustion chamber react with protein thermal decomposition by-products also present within the combustion chamber to mineralize fluorine from polyfluoro and organo fluorine compounds. The protein thermal decomposition by-products functions as a reactive species allowing for further combustion and incineration of PFAS. In one embodiment, as shown in FIG. 3, polyfluoro compounds are combusted within the combustion chamber 28. Optionally, a fossil fuel may be added to the combustion chamber.

The above-described process to convert or degrade hazardous compounds to less hazardous substances includes controlling higher concentrations of nitrogen oxides (NOX), CO, CO₂, nitrogenous/ammonium combustion by-products, nitrogen free radicals and other non-nitrogen containing free radical intermediate combustion reactants in the combustion gasses of the combustion of high protein organic material. The concentration of these combustion by-products within the combustion chamber is controlled to react and convert the carbon-fluoride bonds in PFAS compounds to nitrogen, carbon dioxide/carbon monoxide, hydrogen fluoride (HF) and various mineral fluoride salts based upon the cations available in the fuel. The cations present within the combustion chamber vary upon the type of high protein fuel used and typically include calcium, sodium, potassium, phosphorus and many others at various concentrations. The combination of these by-products within further combustion reactions allows for the break-down and degradation of PFAS compounds. This break-down and degradation of PFAS compounds occurs more quickly and at lower temperatures than current processes for degrading PFAS compounds. For example, while incineration is an acceptable way to destroy PFAS compounds, it traditionally requires higher temperatures (i.e., temperatures above 999° C.) and/or high pressures and longer residence times of greater than one second. These parameters require more sophisticated equipment design and greatly increase the cost and specificity of the type of incineration equipment needed. The present process, in utilizing the high nitrogen content naturally present in high protein organic fuel by-products and excess water injected within the combustion chamber, takes advantage of a novel combustion environment created for the combustion of non-auto-combustible high protein organic materials to degrade PFAS compounds at lower temperatures (i.e., 999° C. or less) for shorter periods of time (i.e., less than 1 second) and lower pressures (i.e., close to atmospheric pressure). This novel combustion environment is not typically achieved or encountered due to the difficult nature of protein combustion. By controlling the excess water, carbon monoxide (CO), nitrogen oxides (NOX), nitrogenous/ammonium combustion by-products, nitrogen free radicals, other non-nitrogen containing free radical intermediate combustion reactants and minerals contained in ash, the incineration of PFAS as a subsequent step to the combustion of high protein organic materials can be optimized.

Examples of polyfluoro compounds used as reactants within the combustion chamber of the above-described process are provided in Table I below.

TABLE I Compound name Abbreviation Type PFAS perfluorododecanoic acid PFDoA PFAS perfluoroundecanoic acid perfluorodecanoic acid PFDA PFAS perfluorononanoic acid PFNA PFAS perfluorooctanoic acid PFOA PFAS perfluoroheptanoic acid PFHpA PFAS perfluorohexanoic acid PFHxA PFAS Perfluoro-3,5-dioxahexanoic acid PFO2HxA perfluoropentanoic acid PFPeA PFAS perfluorobutanoic acid PFBA PFAS perfluoropropanoic acid PFAS trifluoroethanoic acid TFA PFAS Perfluoroethoxypropyl carboxylic acid PEPA PFAS perfluorooctanesulfonic acid PFOS PFAS perfluoroheptanesulfonic acid PFAS perfluorohexanesulfonic acid PFHxS PFAS perfluoropentanesulfonic acid PFAS perfluorobutanesulfonic acid PFBS PFAS perfluoropropanesulfonic acid PFAS trifluoroethanesulfonic acid PFAS trifluoromethanesulfonic acid (triflic acid) PFAS Nonafluorobutanesulfonyl fluoride NfF PFAS N-ethyl-perfluorooctanesulfonamide N-ethyl-perfluorooctanesulfonoamidoethanol PFAS ammonium salt of GenX PFAS hexafluoropropylene oxide dimer acid Perfluoro-2-methoxyacetic acid PFMOAA 2,2-Difluoro-2-(trifluoromethoxy) acetic acid Heptafluoropropyl 1,2,2,2- E1(GenX byproduct) 1,1,1,2,2,3,3-Heptafluoro- tetrafluoroethyl ether 3-(1,2,2,2-tetrafluoroethoxy)propane hexafluoropropylene oxide dimer acid HFPO-DA PFAS Perfluorooctanesulfonamide FOSA/PFOSA 1,1,2,2,3,3,4,4,5,5,6,6,7,7,8,8,8- Heptadecafluoro-1-octanesulfonamide Perfluoro-3,5,7-trioxaoctanoic acid PFO3OA 2-[[Difluoro(trifluoromethoxy) methoxy]diflouromethoxy]- 2,2-difluoroacetic acid Perfluoro-3,5,7,9-tetraoxadecanoic acid PFO4DA 2,2,4,4,6,6,8,8,10,10,10-Undecafluoro- 3,5,7,9-tetraoxadecanoic acid Perfluoro-3,5,7,9,11-pentaoxadodecanoic acid PFO5DoDA C7HF13O7 Perfluorooctane sulfonamidoethanol- SAmPAP diester based phosphate (SAmPAP) esters Chlorodifluoroacetic acid CDFA fluorinated acrylics Nafion byproduct 1 C7HF13O5S Nafion byproduct 2 C7H2F14O5S 2[1-[Difluoro(1,2,2,2- tetrafluoroethoxy)methyl]-1,2,2,2- tetrafluoroethoxy]-1,1,2,2- tetrafluoroethanesulfonic acid Nafion byproduct 4 C7H2F12O6S 2,2,3,3-tetrafluoro-3-((1,1,1,2,3,3- Hydro-EVE C8H2F14O4 hexafluoro-3-(1,2,2,2- tetrafluoroethoxy)propan-2- yl)oxy)propanoic acid Perfluoromethoxypropyl carboxylic acid PMPA C4HF7O3 1,1,2,2-tetrafluoro-2-(1,2,2,2-tetrafluoro- NVHOS C4H2F8O4S ethoxy)ethane sulfonate Gases/Refrigerants Carbon tetrafluoride CF4 Gas 1,1,1,2-Tetrafluoroethane R-134a gas Difluoromethane CH2F2 R-32 fluoromethane CH3F Freon 41 Fluoroform CHF3 R-23 1,1,1,2-Tetrafluoroethane R-134a pentafluoroethane R-125 Mixture of R-32 and R-125 R-410A 2,3,3,3-Tetrafluoropropene R-1234yf 1,3,3,3-Tetrafluoropropene 1-Chloro-3,3,3-trifluoropropene 1,1-Dichloro-1-fluoroethane Trichlorofluoromethane CFC-11 Freon 11 Dichlorodifluoromethane CFC-12 Freon 12 1,1,2-Trichloro-1,2,2-trifluoroethane CFC-113 1,2-Dichlorotetrafluoroethane CFC-114 Cryoflurane Chloropentafluoroethane CFC-115 Bromochlorodifluoromethane halon 1211 Bromotrifluoromethane halon 1301 1,2-dibromotetrafluoroethane halon 2402 Chloro(trifluoro)methane CFC-13 Freon 13 Pentachlorofluoroethane CFC-111 1,1,2,2-Tetrachloro-1,2-difluoroethane CFC-112 1,1,1,2,2,3,3-Heptachloro-3- CFC-211 fluoropropane Hexachlorodifluoropropane CFC-212 1,1,1,3,3-Pentachloro-2,2,3- CFC-213 trifluoropropane 1,2,2,3-Tetrachloro-1,1,3,3- CFC-214 tetrafluoropropane 1,1,1-Trichloro-2,2,3,3,3- CFC-215 pentafluoropropane 1,2-Dichloro-1,1,2,3,3,3- CFC-216 hexafluoropropane 1-Chloro-1,1,2,2,3,3,3- CFC-217 heptafluoropropane 1,1-Dichloro-1-fluoroethane HCFC-141b Dichlorofluoromethane HCFC-21 R-21 Chlorodifluoromethane HCFC-22 R-22 Chlorofluoromethane HCFC-31 1,1,1,2-Tetrachloro-2-fluoroethane HCFC-121 1,1,2-Trichloro-2,2-difluoroethane HCFC-122 2,2-Dichloro-1,1,1-trifluoroethane HCFC-123 1-Chloro-1,2,2,2-tetrafluoroethane HCFC-124 1,1,2-Trichloro-2-fluoroethane HCFC-131 Dichlorodifluoroethane HCFC-132 1-Chloro-1,2,2-Trifluoroethane HCFC-133 1,2-Dichloro-1-fluoroethane HCFC-141 1-Chloro-1,2-difluoroethane/ HCFC-142 1-Chloro-1,1-difluoroethane 1,1,1,2,2,3-Hexachloro-3- HCFC-221 fluoropropane Pentachlorodifluoropropane HCFC-222 Tetrachlorotrifluoropropane HCFC-223 Trichlorotetrafluoropropane HCFC-224 Dichloropentafluoropropane HCFC-225 Chlorohexafluoropropane HCFC-226 Pentachlorofluoropropane HCFC-231 Tetrachlorodifluoropropane HCFC-232 Trichlorotrifluoropropane HCFC-233 Dichlorotetrafluoropropane HCFC-234 Chloropentafluoropropane HCFC-235 Tetrachlorofluoropropane HCFC-241 Trichlorodifluoropropane HCFC-242 Dichlorotrifluoropropane HCFC-243 Chlorotetrafluoropropane HCFC-244 Trichlorofluoropropane HCFC-251 Dichlorodifluoropropane HCFC-252 Chlorotrifluoropropane HCFC-253 Dichlorofluoropropane HCFC-261 Chlorodifluoropropane HCFC-262 Chlorofluoropropane HCFC-271 Polymers Polytetrafluoroethylene PTFE Polyvinylfluoride PVF polyvinylidene fluoride PVDF polychlorotrifluoroethylene PCTFE Nafion C7HF13O5S•C2F4 Various formulas perfluoroalkoxy polymer PFA fluorinated ethylene-propylene FEP polyethylenetetrafluoroethylene ETFE polyethylenechlorotrifluoroethylene ECTFE Viton FKM? Tetrafluoroethylene propylene FEPM Perfluoropolyether PFPE Krytox Monomers/ Hexafluoropropylene oxide HFPO fluorotelomer Hexafluoropropylene HFPO-TA oxide trimer acid tetrafluoroethylene TFE PTFE precursor Fluorotelomer perfluoroethyl iodide CF3CF2I perfluoroalkyl iodide Telomer alcohol Telomer thiol Telomer olefin Polymeric products and non-reacted reactants 1,1-Difluoroethylene 6:2 Fluorotelomer sulfonic acid 6:2 FTSA 3,3,4,4,5,5,6,6,7,7,8,8,8-Tridecafluoro- 1-octanesulfonic acid 6:2 Fluorotelomer alcohol 6:2 FTOH 3,3,4,4,5,5,6,6,7,7,8,8,8- Tridecafluoro-1-octanol 6:2 Fluorotelomer sulfonamide 6:2 FTAB N-(Carboxymethyl)-N,N-dimethy1-3- alkylbetaine [[(3,3,4,4,5,5,6,6,7,7,8,8,8- tridecafluorooctyl)sulfonyl]amino]-1- propanaminium, inner salt 6:2 Fluorotelomer carboxylic acid 6:2 FTCA 3,3,4,4,5,5,6,6,7,7,8,8,8- Tridecafluorooctanoic acid 5:3 Fluorotelomer carboxylic acid 5:3 FTCA 4,4,5,5,6,6,7,7,8,8,8- Undecafluorooctanoic acid 8:2 Fluorotelomer sulfonic acid 8:2 FTSA 3,3,4,4,5,5,6,6,7,7,8,8,9,9,10,10,10- Heptadecafluoro-1-decanesulfonic acid 8:2 Fluorotelomer alcohol 8:2 FTOH 3,3,4,4,5,5,6,6,7,7,8,8,9,9,10,10,10- Heptadecafluoro-1-decanol Fluorinated end PFOS Perfluorooctanesulfonyl fluoride PFOSF perfluorohexanesulfonyl fluoride perfluorodecanesulfonyl fluoride Pesticides N-Ethyl- Sulfuramid CAS #: 4151-50-2 1,1,2,2,3,3,4,4,5,5,6,6,7,7,8,8,8- heptadecafluoro-1-octanesulfonamide Pharmaceuticals Isoflurane Sevoflurane Desflurane Droperidol Enflurane Flurnazenil Halophane Methoxyflurane Midazolam Citalopram Escitaloprarm Fluoxetine HCl Fluvoxamine maleate Paroxetine Progabide Fluticasone propionate Bioaccumlative Dexamethasone fluoroquinolones e.g. Ciprofloxacin Proprietary 3M Novec ™ Fluorosurfactant FC-4430 3M-St. Paul, MN 3M Novec ™ Fluorosurfactant FC-4432 3M-St. Paul, MN AFFF 6:2 Chlorinated polyfluorinated “F-35B” CAS #: 73606-19-6 ether sulfonate 3H-Perfluoro-3-[(3-methoxy-propoxy) “ADONA” CAS #: 958445-44-8 propanoic acid], ammonium salt OMNOVA PolyFox PF-159 Omnova-Beachwood, OH OMNOVA PolyFox . . . Omnova-Beachwood, OH Chemguard S-111 Chemguard-Marinette, WI Chemguard S-151 Chemguard-Marinette, WI Chemguard S-103A Chemguard-Marinette, WI Chemguard S-106A Chemguard-Marinette, WI Chemguard S-216M Chemguard-Marinette, WI Chemguard S-228M Chemguard-Marinette, WI Chemguard S-208M Chemguard-Marinette, WI Chemguard S-500 Chemguard-Marinette, WI Chemguard S-550 Chemguard-Marinette, WI Chemguard S-550-100 Chemguard-Marinette, WI Chemguard S-554 Chemguard-Marinette, WI Chemguard S-554-100 Chemguard-Marinette, WI Chemguard S-559 Chemguard-Marinette, WI Chemguard S-559-100 Chemguard-Marinette, WI Chemguard S-760P Chemguard-Marinette, WI Chemguard S-761P Chemguard-Marinette, WI Chemguard S-764P Chemguard-Marinette, WI Chemguard S-764P-14A Chemguard-Marinette, WI Chemguard S-761P-100 Chemguard-Marinette, WI Chemguard C335 3% × 3% AR-AFFF Chemguard-Marinette, WI Chemguard C334-LV 3% × 3% Chemguard-Marinette, WI AR-AFFF, Low Viscosity Chemguard C364 3% × 6% AR-AFFF Chemguard-Marinette, WI Chemguard C137 1% × 3% AR-AFFF Chemguard-Marinette, WI Chemguard C137-LT18 1% × 3% Chemguard-Marinette, WI AR-AFFF, Low Temperature Chemguard C337-LT13 3% × 3% Chemguard-Marinette, WI AR-AFFF, Low Temperature Chemguard C1B 1% AFFF Chemguard-Marinette, WI Chemguard C1B-LT29 1% AFFF, Chemguard-Marinette, WI Low Temperature Chemguard C306-MS 3% Chemguard-Marinette, WI Military Spec AFFF Chemguard C606-MS 6% Chemguard-Marinette, WI Military Spec AFFF Chemguard C3B 3% AFFF Chemguard-Marinette, WI Chemguard C3B-LT29 3% AFFF, Chemguard-Marinette, WI Low Temperature Chemguard C6B 6% AFFF Chemguard-Marinette, WI Chemguard C3IC1 3% AFFF, ICAO C Chemguard-Marinette, WI Chemguard C3IB2 3% AFFF, ICAO B Chemguard-Marinette, WI Chemguard C6IC1 6% AFFF, ICAO C Chemguard-Marinette, WI Chemguard C6IB2 6% AFFF, ICAO B Chemguard-Marinette, WI Capstone ™ FS-51 Amphoteric fluorosurfactant- Chemours-Wilmington, DE Zonyl ® 1033D Sigma Aldrich-St. Louis, MO Foraperle ® 225 DuPont-Wilmington, DE

Examples of compounds resulting from the reaction of polyfluoro compounds within the combustion chamber are provided within Table below,

TABLE II Compound Phase at Class name Abbreviation 1600 F. Notes HF Hydrogen fluoride HF Gas toxic From Ash Calcium fluoride CaF2 Solid Analysis ↓ Silicon tetrafluoride SiF4 Gas Aluminum fluoride AlF3 Solid Titanium (III) trifluoride TiF3 Solid Titanium (IV) TiF4 Liquid tetrafluoride Iron (III) fluoride FeF3 Solid Magnesium fluoride MgF2 Solid Potassium fluoride KF Liquid Sodium fluoride NaF Solid Sulfur hexafluoride SiF6 Gas Unstable Sulfur decafluoride S2F10 Gas Unstable Sulfur tetrafluoride SF4 Gas Unstable Sulfur difluoride SF2 Gas Unstable Disulfur difluoride S2F2 Gas Unstable Disulfur tetrafluoride S2F4 Gas Unstable Phosphorus trifluoride PF3 Gas toxic Phosphorus pentafluoride PF5 Gas toxic Diphosphorus P2F4 Gas tetrafluoride Strontium (II) fluoride SrF2 Solid Barium fluoride BaF2 Solid Manganese (II) fluoride MnF2 Liquid Manganese (III) fluoride MnF3 Decomposed Manganese (IV) fluoride MnF4 Decomposed Minerals Fluoroapatite Ca5FO12P3 Acuminite SrAlF4(OH)·(H2O) Artroeite PbAlF3(OH)2 Baraite (ammonium (NH4)2SiF6 Decomposed fluorosilicate) to HF and SiF6 Bultfonteinite Ca2SiO2F4 Creedite Ca3Al2SO4F10 Cryolite Na3AlF6 Solid Fluorocaphite (Ca, Sr, Ce, Na)5(PO4)3F Kogarkoite Na3SO4F Neighborite NaMgF3 Sonolite Mn9(SiO4)4F2 Thomsenolite NaCaAlF6·H2O Wagnerite (Mg, Fe)2PO4F Zharchikhite AlF(OH)2 Other Zinc fluoride ZnF2 Solid elements ↓ Beryllium fluoride BeF2 Liquid Lithium fluoride LiF Liquid Rubidium fluoride RbF Liquid Cesium fluoride CsF Liquid Radium fluoride RaF2 Zirconium (IV) fluoride ZrF4 Solid Mercury (II) fluoride HgF2 Silver (I) fluoride AgF Liquid Copper (II) fluoride CuF2 Liquid Nickel (II) fluoride NiF2 Solid Chromium (II) fluoride CrF2 Solid oxidizes in air Chromium (III) fluoride CRF3 Solid Cobalt (II) fluoride CoF2 Solid Vanadium (III) fluoride VF3 Solid Vanadium (IV) fluoride VF4 Decomposes at 325 C. Scandium (III) fluoride ScF3 Solid Boron trifluoride BF3 Gas Will hydrolyze to HF Gallium (III) fluoride GaF3 Liquid Platinum tetrafluoride PtF4 Liquid Cadmium fluoride CdF2 Solid Molybdenum (IV) MoF4 fluoride Molybdenum (V) fluoride MoF5 Molybdenum (III) MoF3 Solid fluoride Tantalum (V) fluoride TaF5 Decomposes Palladium (II) fluoride PdF2 Solid Palladium (II, IV) fluoride PdF3 Solid Gold (III) fluoride AuF3 Gas Reactive Tin (II) fluoride SnF2 Gas Tin (IV) fluoride SnF4 Liquid Lead tetrafluoride PbF4 Liquid Bismuth (III) fluoride BiF3 Liquid Cerium (III) trifluoride CeF3 Solid

Although certain specific steps and devices for performing the steps of the process of the present disclosure have been disclosed above, it will be apparent to one of ordinary skill in the art that other steps and devices may be used without departing from the scope of the present disclosure indicated in the appended claims. It will also be apparent that the present disclosure may be applied to other types of high protein non-auto-combustible organic materials. It will also be apparent that the present disclosure may be applied to other processes, in addition to those disclosed herein. For example, in addition to Brewers Spent Grains (termed BDG in the art) described above, the present disclosure may be applied to Distillers Spent Grain (DDG) and any fermentation process of grains that produce alcohol. 

We claim:
 1. A process for converting hazardous compounds to less hazardous substances comprising the following steps: 1) providing a non-auto-combustible organic material, wherein the organic material is a high protein organic material having a protein content of about 10%, on a dry weight basis (DWB) or greater; 2) optionally mechanically removing liquid and soluble components from the high protein organic material; 3) optionally applying heat to dry the organic material to reduce its moisture content to ten percent (10%) or less by weight; 4) pulverizing the high protein organic material to reduce the high protein organic material to a particle size of less than 2 mm, wherein the pre-combustion steps of 2) optionally mechanically removing liquid and soluble components from the high protein organic material, 3) optionally applying heat to dry the organic material to reduce its moisture content to ten percent (10%) or less by weight and, 4) pulverizing the high protein organic material to reduce the high protein organic material to a particle size of less than 2 mm may occur in any order; 5) separating particles of the high protein organic material during a combustion phase to inhibit their cohesion into an integrated mass by spraying the particles into a combustion chamber; 6) simultaneously injecting steam into the combustion chamber to enhance combustion characteristics of the high protein organic material; 7) allowing protein thermal decomposition by-products to react with nitrogen oxides (NOX) within the combustion chamber to form water (H₂O) and nitrogen (N₂); wherein nitrogen oxide (NOX) production ranges from about 100 parts per million (ppm) to about 300 parts per million (ppm) or more; wherein protein thermal decomposition by-products remaining after combustion include ammonium, nitrogenous hydrocarbons, carbon monoxide (CO), carbon dioxide (CO₂), nitrogen oxides (NOX), nitrogen free radicals, nitrogen cations and other non-nitrogen containing free radical intermediate combustion reactants in the combustion gasses; 8) controlling protein thermal decomposition by-products including nitrogen oxide (NOX) production produced during combustion within the combustion chamber; and 9) incinerating polyfluoro compound impurities present within the processed non-autocombustible high protein organic material in the combustion chamber and/or adding and incinerating polyfluoro compounds within the combustion chamber, wherein the protein thermal decomposition by-products functions as a reactive species to incinerate polyfluoro compounds to degrade hazardous polyfluoro compounds into less hazardous substances.
 2. The process defined in claim 1, wherein protein decomposition by-product ash resulting from the combustion of high protein organic materials contains about 300 ppm or more ammonium, nitrogenous hydrocarbons, carbon monoxide (CO), carbon dioxide (CO₂), nitrogen oxides (NOX), nitrogen free radicals, nitrogen cations, and other non-nitrogen containing free radical intermediate combustion reactants.
 3. The process defined in claim 1, wherein pulverizing, pressing, applying heat to dry the high protein organic material particles, spraying particles into the combustion chamber and injecting steam into the combustion chamber degrades the proteins contained within the particles and denatures them by allowing nitrogen cross-linking and other cross-linking reactions to occur within the particles, allowing the particles to complete all of the cross-linking ability before the particles contact other particles.
 4. The process defined in claim 3, wherein cross-linking of the high protein organic material particles is prevented by prematurely initiating cross-linking reactions of the nitrogen bonds and other cross linking reactions while the particles are being agitated and wherein the high protein organic material particles no longer adhere to each other, thereby arresting the particles tendency to adhere to each other within the combustion chamber via nitrogen bond cross-linkage and other cross-linkage reactions.
 5. The process defined in claim 4, wherein the step of separating the high protein organic material by spraying the processed high protein organic material into the combustion chamber is effected through use of a pneumatic stoker.
 6. The process defined in claim 5, wherein spraying the particles of the high protein organic material into the combustion chamber by the pneumatic stoker keeps the particles separated in the combustion chamber long enough to allow heat transfer provided by the combustion process to quickly dry and then degrade proteins present within the high protein organic material and to prevent nitrogen cross linking and other cross linking reactions between the particles that would have the particles adhere to each other.
 7. The process defined in claim 6, wherein the particles of the high protein organic material are separated and dispersed within the combustion chamber and ignited and burned while in suspension and separated from each other before they land and adhere to each other.
 8. The process defined in claim 7, wherein the non-auto-combustible high protein organic material is rendered combustible without the addition of other combustible fuels or additives.
 9. The process defined in claim 8, wherein the polyfluoro compound impurities and polyfluoro compounds comprise polyfluoroalkyl compounds and perfluoralkyl compounds (PFAS), organic fluoride (organo fluorine) compounds and non-organic mineralized organo fluorine compounds.
 10. The process defined in claim 9, wherein the PFAS substances further comprise perfluorooctanoic acid (PFOA) and perfluorooctane sulfonate (PFOS).
 11. The process of claim 10, further comprising controlling the concentration of ammonium, nitrogenous hydrocarbons, carbon monoxide (CO), carbon dioxide (CO₂), nitrogen oxides (NOX), nitrogen cations, nitrogen free radicals and other non-nitrogen containing free radical intermediate combustion reactants in the combustion gasses within the combustion chamber.
 12. The process of claim 11, wherein the concentration of protein thermal decomposition by-products and excess water within the combustion chamber is controlled to react and convert carbon-fluoride bonds in PFAS compounds to nitrogen, carbon dioxide/carbon monoxide, hydrogen fluoride (HF) and various inorganic fluoride containing salts and/or minerals based upon cations present in the fuel.
 13. The process of claim 12, wherein the incineration of PFAS compounds within the combustion chamber occurs at a temperature of 999° C. or below.
 14. The process of claim 13, wherein the incineration of PFAS compounds within the combustion chamber has a residence time of 1 second or less at a temperature of 999° C.
 15. The process of claim 14, wherein the nitrogen cations and concentrations of nitrogen cations present within the combustion chamber after combustion of the high protein organic material vary upon the type of high protein fuel used for combustion and comprise at least one of calcium, sodium, potassium, phosphorus, silica and manganese.
 16. The process defined in claim 15, wherein PFAS substances are degraded to an inorganic mineralized form.
 17. The process defined in claim 16, wherein PFAS substances are degraded to calcium fluoride (CaF₂) or hydrogen fluoride (HF).
 18. The process defined in claim 17, wherein the high protein organic material is a biological waste or by-product material, wherein the biological waste or by-product material originates from waste water treatment activated sludge waste and wherein the process comprises the following order of steps: 1) providing a biological waste material or by-product comprising a waste water treatment activated sludge having a protein content of about 10% or greater, on a dry weight basis (DWB); 2) removing water, moisture and other soluble components from the biological waste material or by-product; 3) drying the biological waste material or by-product to reduce the moisture content to 10% or less by weight; 4) pulverizing the biological waste material to reduce the particle size to be less than 2 mm; 5) separating particles of the biological waste material or by-product during the combustion phase to inhibit their cohesion into an integrated mass by spraying the particles into the combustion chamber; 6) simultaneously injecting steam into the combustion chamber, wherein steam is injected to modify and control combustion reactions by reacting with nitrogen within proteins to form intermediate nitrogenous-based protein thermal combustion products which help to maintain regulatory compliance of combustion emissions; 7) controlling protein thermal decomposition by-products including nitrogen oxide (NOX) production, produced during combustion within the combustion chamber, wherein the protein thermal decomposition by-products functions as a reactive species to incinerate PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds; 8) optionally, adding additional PFAS substances in the combustion chamber for further combustion; and 9) incinerating PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds within the combustion chamber, wherein the biological waste or by-product material contains PFAS, organic fluoride (organo fluorine) compounds and/or non-organic mineralized fluorine compounds and/or wherein PFAS, organic fluoride (organo fluorine) compounds and/or non-organic mineralized fluorine compounds are added to the biological waste or by-product material within the combustion chamber for incineration.
 19. The process defined in claim 17, wherein the high protein organic material is hops residue and wherein the process comprises the following steps in the following order: 1) extracting oils and other compounds from the ground hops utilizing mechanical separation techniques or CO2 extraction to obtain a high protein hops waste residue having a protein content of about 25 to about 30 weight percent, on a dry weight basis (DWB); 2) providing the hops waste residue; 3) drying the hops waste residue, wherein the step of drying the hops waste residue comprises the application of heat; 4) grinding the hops waste residue into a powder by pulverizing the hops waste residue to ensure that particles of the hops waste residue have a particle size of less than 2 mm, wherein the step of pulverizing the hops waste residue includes subjecting the hops residue to a mill; 5) agitating the hops waste residue during a combustion phase to separate particles of the hops waste residue by spraying the particles into the combustion chamber to inhibit their cohesion into an integrated mass; 6) simultaneously injecting steam into the combustion chamber to enhance the combustibility of the high protein organic material; 7) controlling protein thermal decomposition by-products including nitrogen oxide (NOX) production, produced during combustion within the combustion chamber, wherein the protein thermal decomposition by-products functions as a reactive species to incinerate PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds; 8) optionally, adding additional PFAS substances in the combustion chamber for further combustion; and 9) incinerating PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds within the combustion chamber, wherein the biological waste or by-product material contains PFAS, organic fluoride (organo fluorine) compounds and/or non-organic mineralized fluorine compounds and/or wherein PFAS, organic fluoride (organo fluorine) compounds and/or non-organic mineralized fluorine compounds are added to the biological waste or by-product material within the combustion chamber for incineration.
 20. The process defined in claim 17, wherein the high protein organic material is a high protein waste or meal from an agricultural source of oil production, waste by-products and by-products from an oil seed pulp processing.
 21. The process defined in claim 20, wherein the high protein organic material comprises an oil seed pulp waste residue, further wherein the process comprises the following order of steps: 1) obtaining an extracted high protein oil seed pulp waste residue having a protein content of about 35%, on a dry weight basis (DWB), a moisture content of ten percent (10%) or less and a particle size less than 2 mm, wherein oil from the oil seed pulp waste residue may or may not be preliminarily extracted; 2) separating and agitating particles of the oil seed pulp waste residue during the combustion phase to inhibit their cohesion into an integrated mass while simultaneously injecting steam into the combustion chamber; 3) controlling protein thermal decomposition by-products including nitrogen oxide (NOX) production, produced during combustion within the combustion chamber, wherein the protein thermal decomposition by-products functions as a reactive species to incinerate PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds; 4) optionally, adding additional organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds in the combustion chamber for further combustion; and 5) incinerating PFAS, organic fluoride (organo fluorine) compounds and non-organic mineralized fluorine compounds within the combustion chamber, wherein the oil seed pulp waste contains PFAS, organic fluoride (organo fluorine) compounds and/or non-organic mineralized fluorine compounds.
 22. The process defined in claim 17, wherein the high protein organic material is one of a high protein animal excreta or a high protein animal meat processing by-product or waste and wherein the process comprises obtaining a pre-processed or “as is” high protein animal excreta or high protein animal meat processing by-product or waste which is non-auto-combustible, wherein the animal excreta has a protein content ranging from about 20% to about 60%, on a dry weight basis (DWB) and the animal meat processing by-product or waste has a protein content ranging from about 35% to about 85% dry weight basis.
 23. A process for converting hazardous compounds to less hazardous substances within a traditional combustion chamber comprising the following steps: 1) providing an auto-combustible organic fuel; 2) providing a non-auto-combustible organic material, wherein the organic material is a high protein organic material having a protein content of about 10%, on a dry weight basis (DWB) or greater; 3) optionally mechanically removing liquid and soluble components from the high protein organic material; 4) optionally applying heat to dry the organic material to reduce its moisture content to ten percent (10%) or less by weight; 5) pulverizing the high protein organic material to reduce the high protein organic material to a particle size of less than 2 mm, wherein the pre-combustion steps of 3) optionally mechanically removing liquid and soluble components from the high protein organic material, 4) optionally applying heat to dry the organic material to reduce its moisture content to ten percent (10%) or less by weight and, 5) pulverizing the high protein organic material to reduce the high protein organic material to a particle size of less than 2 mm may occur in any order; 6) injecting the auto-combustible organic material into a combustion chamber; 7) spraying the non-auto-combustible high protein organic material into the combustion chamber through use of a pneumatic stoker to separate particles of the high protein organic material and inhibit their cohesion into an integrated mass during combustion; 8) simultaneously injecting steam into the combustion chamber to enhance combustion characteristics of the high protein organic material; 9) allowing protein thermal decomposition by-products to react with nitrogen oxides (NOX) within the combustion chamber to form water (H₂O) and nitrogen (N₂), wherein nitrogen oxide (NOX) production ranges from about 100 parts per million (ppm) to greater than 300 parts per million (ppm), wherein protein thermal decomposition by-products remaining after combustion include ammonium, nitrogenous hydrocarbons, carbon monoxide (CO), carbon dioxide (CO₂), nitrogen oxides (NOX), nitrogen cations, nitrogen free radicals, and other non-nitrogen containing free radical intermediate combustion reactants in the combustion gasses; 10) controlling protein thermal decomposition by-products including nitrogen oxide (NOX) production, produced during combustion within the combustion chamber; and 11) incinerating polyfluoro compound impurities present within the processed non-autocombustible high protein organic material in the combustion chamber and optionally, adding and incinerating additional polyfluoro compounds within the combustion chamber as an additional or alternative step, wherein the protein thermal decomposition by-products functions as a reactive species to incinerate polyfluoro compounds to degrade hazardous polyfluoro compounds into less hazardous substances. 